烯烃转化单元中英文对照工艺(共15页).doc

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1、精选优质文档-倾情为你奉上OCU PROCESS DESCRIPTION烯烃转化单元工艺说明1.1 Plant Composition 装置组成Shanxi Coking Company Ltd. intends to build a 104 kta Olefins Conversion Unit (OCU) in the Fine Coal Chemical Zone, Zhaocheng, Hongdong County, Shanxi Province, P.R.C. The capacity of the unit will be 104 kta polymer grade propy

2、lene based on 8000 operation hours per year. The plant feed will be the Mixed C4/C5 product from the Light Olefins Recovery Unit (LORU). In addition, the plant also produces the following by-products:山西焦化股份有限公司计划在中国山西省洪洞县赵城镇精细煤化工园区建设一套10.4万吨/年烯烃转换装置（OCU）。该装置的生产能力为10.4万吨/年聚合级丙烯，年开工率8000小时。装置进料将采用来自轻烯

3、烃回收装置（LORU）的混合C4/C5产品。另外，该装置还生产以下副产品：Mixed C4 to N-Butene Unit 混合C4，输送至正丁烯装置C4+ by-product Stream C4+副产品流SHU Vent Gas 选择加氢装置放空气体OCU Vent Gas 烯烃转换装置（OCU）放空气体 DME Purge 二甲醚吹扫气体The plant shall be flexible to handle 60-120% of normal capacity and designed for 36 months between turnaround. The plant shal

4、l be designed for an operating life of 20 years. 本装置的操作弹性范围为正常生产能力的60-120%，并且装置大修的间隔应为36个月。装置的使用年限应设计为20年。The OCU unit consists of the following sections烯烃转化装置由以下工段组成：DME Removal 二甲醚脱除单元1st Stage Selective Hydrogenation Unit (SHU1)1段选择加氢单元（SHU1）2nd Stage Selective Hydrogenation Unit (SHU2)2 段选择加氢单元（

5、SHU2）Debutanizer 脱丁烷塔OCU Feed Treatment 烯烃转换装置进料处理OCU Reactors 烯烃转换装置反应器Deethylenizer 脱乙烯塔Depropylenizer 脱丙烯塔Regeneration System 再生系统1.2 Process Flow Description 工艺流程描述1.2.1 DME Removal 二甲醚脱除单元Mixed C4s/C5s from LORU are fed on flow control to the DME Removal Column. This column removes most of the

6、DME and Light Ends contained in the Mixed C4/C5 Feed. 来自轻烯烃回收装置的混合C4/C5在流量控制下进入二甲醚脱除塔（299-T-3101），以脱除混合C4进料中的DME和轻组分。 The DME Removal Column pressure is set to allow the column overhead to be condensed against Cooling Water and reboiled using LP2 Pressure Steam. The tower net overhead is a small ven

7、t stream containing the DME removed from the feed, as well as any light compounds in the feed. The net overhead vent stream is recycled on flow control along with the 1st Stage Selective Hydrogenation (SHU-1) vent stream to the Charge Gas Compressor Second Stage Suction Drum.DME脱除塔的压力设定为能够通过冷却水对塔顶排放

8、气进行冷凝，并通过低低压（LP2）蒸汽对其进行重沸。塔顶净排放气流量不大，含有从进料中脱除的DME以及进料中的轻组分。在流量控制下，塔顶净排放气与第一段选择加氢装置（SHU-1）排放气循环至进料气压缩机二段入口罐。Heat input to the tower is controlled by a flow controller on the LP2 steam-heated reboiler. Periodic analysis of the bottoms assures the bottoms product contains no more than 5 wt ppm DME. The

9、 tower bottoms pumped and cooled against Cooling Water and sent on flow control, reset by level control, to the 1st Stage Selective Hydrogenation Unit.DME脱除塔热量输入通过LP蒸汽加热重沸器的流量控制器进行控制。对塔底物料进行定期分析，确保塔底产物中DME的含量不大于5wppm。塔底物料泵出后，通过冷却水进行冷却，然后在流量控制下（基于塔底液位控制器设定值）送入SHU一段。1.2.2 1st Stage Selective Hydrogena

10、tion (SHU-1)1段选择加氢单元（SHU1）The bottoms of DME column are fed to the SHU Feed Surge Drum. This stream is then pumped to 1st Stage SHU Reactor pressure on flow control, reset by level control, and mixed with a portion of the 1st Stage SHU Reactor effluent recycled back to the feed. This Mixed C4/C5 Fee

11、d stream is heated to the required reactor temperature in a Low-Low Pressure steam-heated heat exchanger and then mixed with Hydrogen on flow-ratio control. 二甲醚脱除塔塔底物料进入选择加氢装置进料缓冲罐，并在流量控制下（基于进料缓冲罐液位控制器设定值）泵送至第一段SHU反应器，与循环回进料的一部分第一段SHU反应器流出物混合。混合C4/C5通过低低压蒸汽加热换热器加热至要求的反应器温度，然后按照流量比与氢气混合。 Hot Mixed C4

12、s/C5s and Hydrogen then pass downflow through the 1st Stage SHU Reactor where butadiene is selectively hydrogenated to n-butenes and pentadienes are selectively hydrogenated to n-butenes and n-pentenes, respectively. Since the selective hydrogenation process is exothermic, a temperature rise occurs

13、across the reactor. The heat of reaction is absorbed by the C4/C5 stream as it passes through the catalyst bed. The reaction product is separated in the 1st Stage SHU Reactor Separator Drum. The vapor from the drum is cooled against Cooling Water to recover C4s/C5s which flow to the separator drum.

14、The remaining vent gas is recycled to the LORU. The liquid from the separator drum is pumped to reactor pressure. Some of the liquid is recycled back to the reactor on flow control and the rest is cooled and fed the 2nd Stage SHU Reactor via flow control reset by the1st Stage SHU Separator Drum leve

15、l controller.The feed temperature to the 2nd Stage Reactor is controlled by by-passing some of the liquid around the 1st Stage SHU Reactor Recycle/Product Cooler. Effluent from the 1st Stage SHU contains about 2300 wt ppm butadiene and pentadienes.热混合C4/C5和氢气然后向下流经第一段SHU反应器，在该反应器中丁二烯通过选择加氢处理被转化为正丁烯，

16、而戊二烯通过选择加氢处理被转化为正丁烯和正戊烯。由于选择加氢反应为放热反应，反应器内部会出现温升。由于反应热沿催化剂床传递，因此使用C4/C5物流对反应热进行吸收。反应产物在第一段SHU反应器分离罐中分离。来自分离罐的部分蒸气由冷却水冷却以回收C4/C5，回收的C4返回分离罐，剩余排放气循环回LORU。分离罐液体通过泵提升至反应器压力，部分液体在流量控制下循环回反应器，剩余液体经冷却后按照第一段SHU分离罐液位控制器设定值以流量控制方式进入第二段SHU反应器。第二段反应器进料温度通过第一段SHU反应器循环物料/产品冷却器的液体旁通阀来进行控制。来自第一段SHU装置的流出物约含有2300wppm

17、的丁二烯和戊二烯。Gradual loss of catalyst activity will occur as the active sites on the catalyst become coked. Regeneration of the catalyst is required when catalyst activity has dropped to the point when the reactor outlet temperature of about 89 is reached. Regeneration requires the catalyst bed to be ta

18、ken offline, drained and purged of hydrocarbons, heated with hot nitrogen and then superheated with steam. Air is metered into the stream to decoke the bed. A final nitrogen purge that contains a controlled amount of hydrogen reduces the catalyst bed. 随着催化剂活性中心逐渐结焦，催化剂将逐渐失去活性。随着催化剂活性逐步降低，当反应器出口温度达到约

19、89C时，就需要对催化剂进行再生。催化剂再生时要求催化剂床离线，并将反应器内部烃物料排出并吹扫干净，使用热氮气进行加热，然后使用蒸汽进行过热。以流量控制方式向物流中引入空气，以对床层进行清焦。使用含一定量氢气的氮气对催化剂床进行还原。 A spare reactor is provided so that production can be maintained while one reactor is regenerated. A SHU Reactor Regeneration Electric Heater is used to heat the hot gas mixtures use

20、d to regenerate the 1st Stage SHU Reactor catalyst.设置备用反应器可以保证在对其中一台反应器进行再生期间不会中断装置运行。SHU反应器再生电加热器用于加热第一段SHU反应器催化剂再生所需的热混合气。1.2.3 2nd Stage Selective Hydrogenation (SHU-2)2段选择加氢单元（SHU2）The 1st Stage SHU effluent contains about 2300 wt ppm butadiene and Pentadienes combined. The total butadiene and p

21、entadiene content is further reduced to 50 wt ppm in the 2nd Stage SHU. The 2nd Stage SHU is a once-thru system with feed heating and effluent cooling.第一段SHU流出物中含有约2300wtppm的丁二烯和戊二烯，在第二段SHU装置中，将总的丁二烯和戊二烯含量进一步降至50wtppm。第二段SHU是一个单程系统，在系统中完成进料加热和流出物冷却。1st Stage SHU effluent after pumping and mixing wit

22、h hydrogen on flow-ratio control is heated to the hydrogenation reactor temperature in a LP2 steam-heated heat exchanger and then hot mixed C4/C5s and hydrogen then pass upflow through the 2nd Stage SHU Reactor where the remaining butadiene is selectively hydrogenated to n-butenes and pentadienes to

23、 respective pentenes. Since the selective hydrogenation process is exothermic, a temperature rise occurs across the reactor. The heat of reaction is absorbed by the C4/C5 stream as it passes through the catalyst bed. The reaction product is immediately cooled in the 2nd Stage SHU Reactor Effluent Co

24、oler and flows to the OCU Fresh/Recycle C4/C5 Surge Drum through a back pressure controller. The controller maintains the 2nd stage SHU Reactor in the liquid phase.将第一段SHU流出物泵出，并按照规定的流量比与氢气混合，然后通过LP2蒸汽加热换热器加热至加氢反应器温度。热混合C4/C5和氢气然后向上流经第二段SHU反应器，在该反应器中，剩余丁二烯通过选择加氢处理被转化为正丁烯，戊二稀转化为正戊烯。由于选择加氢反应为放热反应，反应器内

25、部会出现温升。由于反应热沿催化剂床传递，因此使用C4/C5物流对反应热进行吸收。反应产物紧接着在第二段SHU反应器流出物冷却器中冷却，然后在背压控制器控制下进入OCU新鲜/循环C4/C5缓冲罐。该背压控制器用于使第二段SHU反应器中物料保持为液相。Gradual loss of catalyst activity will occur as the active sites on the catalyst become coked. Regeneration of the catalyst is required when catalyst activity has dropped to th

26、e point when a reactor outlet temperature of about 89 is reached. Regeneration requires the catalyst bed to be taken offline, drained and purged of hydrocarbons, heated with hot nitrogen and then superheated with steam. Air is metered into the stream to decoke the bed. A final nitrogen purge that co

27、ntains a controlled amount of hydrogen reduces the catalyst bed. 随着催化剂活性中心逐渐结焦，催化剂将逐渐失去活性。随着催化剂活性逐步降低，当反应器出口温度达到约89C时，就需要对催化剂进行再生。催化剂再生时要求催化剂床离线，并将反应器内部烃物料排出并吹扫干净，使用热氮气进行加热，然后使用蒸汽进行过热。以流量控制方式向物流中引入空气，以对床层进行清焦。使用含一定量氢气的氮气对催化剂床进行还原。 No spare reactor is provided. When the 2nd Stage SHU Reactor requires

28、 regeneration the 1st stage SHU Reactor is temporarily run in less selective mode to reduce the butadiene and pentadiene content sufficient to feed the OCU.没有提供备用反应器。当需要对第二段SHU反应器进行再生时，应临时降低第一段SHU反应器的选择加氢性能，从而将丁二烯和戊二稀含量降至规定值，以向OCU装置进料。A SHU Reactor Regeneration Electric Heater is used to heat the ho

29、t gas mixtures used to regenerate the 2nd Stage SHU Reactor catalyst.SHU反应器再生电加热器用于加热第二段SHU反应器催化剂再生所需的热混合气。1.2.4 Debutanization 脱丁烷The effluent from SHU-2 is sent to the debutanizer. This column removes C5 components to produce a Mixed C4 stream suitable for feed the OSBL N-butene Unit. 来自二段选择加氢装置的流

30、出物进入脱丁烷塔。该塔脱除C5组分以生产适合进入界区外正丁烯装置的混合C4产品流。 The debutanizer overhead is condensed by cooling water and reboiled by desuperheated LP2 pressure steam. A portion of the liquid from the debutanizer reflux drum is sent as reflux to the tower and the remaining liquid is taken as mixed C4 product, which is s

31、ent to OSBL. The bottoms C5 product is pumped and cooled to 40 by cooling water, before being sent to the OCT Fresh/Recycle C4/C5 Surge Drum.脱丁烷塔塔顶物经冷却水冷凝后通过减温较低压力蒸汽再煮沸。来自脱丁烷塔回流罐液体的一部分进入该塔作为回流，剩余液体抽出作为混合C4产品输送到界区外。塔底C5产品经泵抽出后用冷却水冷却至40，然后输送至OCT新鲜/循环C4/C5缓冲罐。1.2.5 OCT Reactor Feed Treatment 烯烃转换装置进料处理

32、The debutanizer overhead is combined with the Mixed C4 Raffinate from the N-Butene unit (OSBL) and the recycle C4/C5s in the OCT Fresh/Recycle C4/C5 Surge Drum. The Mixed C4s/C5s from this drum are pumped to the OCT reaction pressure and combined with Fresh and Recycle Ethylene, mixed in a static mi

33、xer to dissolve the Ethylene in the liquid C4/C5, then treated in the OCT Reactor Feed Treater.The operating pressure of the treater is such that the Mixed C4+C5/Ethylene feed is in liquid phase.脱丁烷塔塔顶物料与界区外正丁烯装置混合C4的抽余液及循环C4/C5在OCT新鲜/循环C4/C5缓冲罐中混合。来自该罐的混合C4/C5经泵提升至OCT反应器压力，并与新鲜和循环乙烯在静态混合器中混合，以使乙烯溶解

34、在液体C4/C5中，然后在OCT反应器进料处理器中进行处理。处理器设计运行压力能够保证使混合C4+C5乙烯进料保持为液相。 The OCT Reactor Feed Treater is designed to remove trace potential catalyst temporary poisons in the Mixed C4+C5/Ethylene stream that could impair the OCT Reactor performance such as oxygenates, sulfur, alcohols, carbonyls, and/or water.

35、There are two treaters provided in the system. One is normally in operation; while the other is in regeneration or on standby. The treater regeneration initially requires draining of the liquid inventory followed by regeneration using hot Nitrogen from the Regeneration Gas System plus a supplemental

36、 electric heater. The treater effluent passes through a filter to remove any adsorbent dust.OCT反应器进料处理器用于脱除C4+C5乙烯混合进料中的痕量催化剂毒物，如氧合物、羰基化合物、乙醇、硫化合物和/或水，以防止对OCT反应器运行性能造成影响。系统设置两台处理器：一台通常处于运行状态，另一台用于再生目的或作为备用处理器。在对处理器进行再生时，首先对处理器进行排液，然后采用来自再生气系统的热氮气和辅助电加热器进行再生。处理器流出物送入过滤器，以脱除任何吸附剂粉末。1.2.6 OCU Reactors

37、烯烃转换装置反应器In this section, the OCU Reactor feed is heated to the required reaction temperature, passed through the OCU Reactor and cooled prior to OCU reactor effluent fractionation. The main reactions that occur are ethylene plus 2butene forming propylene and ethylene plus 2-pentene forming propylen

38、e plus 1-butene. Some byproducts, primarily C5 to C8 olefins, are also formed by side reactions.在本工段，将OCU反应器进料加热至要求的反应温度后送入OCU反应器，并且在将OCU反应器流出物送入精馏塔之前应先进行冷却。主要OCU反应是以乙烯和2-丁烯作为原料经反应生成丙烯以及乙烯和2-戊烯反应生成丙烯和1-丁烯。另外，也发生一些副反应，所生成的副产品主要为C5-C8烯烃。The OCU reactor feed is vaporized and heated to the required OCU

39、Reactor temperature in an OCT Reactor Feed/Effluent Exchanger followed by the OCT Reactor Feed Heater. The OCU reaction occurs in a fixed bed catalytic reactor. The OCU catalyst is a mixed catalyst bed comprised of magnesium oxide and tungsten oxide on silica. The reactions occurring are essentially

40、 isothermal.OCU反应器进料先由OCT反应器进料/流出物换热器进行汽化，然后再通过OCT反应器进料加热器加热至要求的OCU反应器温度。OCU反应在固定床催化反应器中进行。OCU催化剂为混合催化剂，由氧化镁和以硅藻土为载体的氧化钨制备而成。所有反应基本上均为等温反应。Prior to entering the recovery section, the OCU Reactor effluent is cooled by interchange with reactor feed followed by the OCT Reactor Effluent Cooler against C

41、ooling Water.在进入回收工段之前，OCU反应器流出物首先与OCU反应器进料进行换热，然后在OCT反应器流出物冷却器中通过冷却水进行冷却。Regeneration of the OCU Reactor requires the catalyst bed to be taken offline, purged of hydrocarbons, and heated with hot Nitrogen. A nitrogen-air mixture is then fed to the reactor to decoke the bed. A nitrogen purge, which

42、contains a controlled amount of hydrogen, reduces the catalyst bed. A high temperature Nitrogen desorption step follows to remove any traces of oxygen and water from the bed. Hot regeneration gases for the regeneration of the OCU Reactor are provided by the Regeneration Gas Heater.在对OCU反应器进行再生时需要使催化

43、剂床离线、将烃物料吹扫干净、使用热氮气进行加热。然后，向OCU反应器注入氮气-空气混合气体以对床层进行清焦。使用含一定量氢气的氮气对催化剂床进行还原。随后进行热氮气解吸，以将催化剂床的痕量氧气和水分脱除。OCU反应器再生用高温再生气由再生气加热器提供。1.2.7 Deethylenizer 脱乙烯塔The OCU Reactor effluent is chilled by vaporizing a portion of the Recycle Ethylene in the Deethylenizer Feed Chiller. The chilled feed then flows to

44、the Deethylenizer column.OCU反应器流出物通过在脱乙烯塔进料深冷器中对一部分循环乙烯进行汽化来实现冷却。然后，已冷却进料流入脱乙烯塔。The Deethylenizer pressure is selected to recycle vent gas from the reflux drum and to allow the overhead to condense against -24 Propylene Refrigerant from the Propylene Refrigeration System of the LORU. A small vent ga

45、s stream containing Hydrogen, Methane, and Ethylene flows from the reflux drum on flow control to the LORU for recovery.脱乙烯塔设计压力能够对来自回流罐的排放气进行循环，并使用来自LORU装置丙烯制冷系统的-24C丙烯冷剂对塔顶物料进行冷凝。一小股含有氢气、甲烷和乙烯的排放气以流量控制方式从回流罐流入LORU进行回收。Fresh Ethylene liquid is fed to the Deethylenizer Reflux Drum. The bulk of the t

46、ower overhead is condensed against Propylene Refrigerant and sent to the Deethylenizer Reflux Drum. Liquid from the reflux drum is split, with a portion pumped to OCU Reactor Feed Treater pressure to supply Recycle Ethylene, and a portion pumped separately to supply tower reflux on flow control. The

47、 net Fresh plus Recycle Ethylene is pumped and sent to the Deethylenizer Feed Chiller on flow control. A portion of the Recycle Ethylene stream is vaporized in this heat exchanger. The rest bypasses the feed chiller on temperature control, in order to maintain the OCU Reactor feed in the liquid phas

48、e at the outlet of the OCU Reactor Feed Treater. The Recycle Ethylene stream then mixes with Fresh and Recycle C4s/C5s at the OCU Reactor Feed Treater Mixer and flows to the OCU Reactor Feed Treaters.新鲜乙烯液体送入脱乙烯塔回流罐。大量脱乙烯塔塔顶物料经丙烯冷剂冷凝后送入脱乙烯塔回流罐。脱乙烯塔回流罐中的液体分为两股：一股液体泵送至OCU反应器进料处理器作为循环乙烯，另外一股液体以流量控制方式泵送回脱乙烯塔作为回流。净新鲜乙烯和循环乙烯以流量控制方式泵送至脱乙烯塔进料深冷器。在脱乙烯塔进料深冷器中，一部分循环乙烯被汽化，而剩余循环乙烯以温度控制方式进入脱乙烯塔进料深冷器旁路，以确保将来自OCU反应器进料处理器出口的OCU反应器进料保持为液相。然后，循环乙烯通过OCU反应器进料处理器混合器与新鲜和循环C4、C5混合后流入OCU反应器进料处理器。 The tower is reboiled by LP2 Steam with the bottoms product flowing to th