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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 propylene 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 shall 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（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 Proce Flow Description 工艺流程描述 1.2.1 DME Removal
二甲醚脱除单元
Mixed C4’s/C5’s from LORU are fed on flow control to the DME Removal Column.This column removes most of the 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 preure is set to allow the column overhead to be condensed against Cooling Water and reboiled using LP2 Preure Steam.The tower net overhead is a small vent 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 Compreor 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 aures the bottoms product contains no more than 5 wt ppm DME.The 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 Hydrogenation(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 preure 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 Feed stream is heated to the required reactor temperature in a Low-Low Preure 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’s/C5’s and Hydrogen then pa 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 proce is exothermic, a temperature rise occurs acro the reactor.The heat of
reaction is absorbed by the C4/C5 stream as it paes 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 C4’s/C5’s which flow to the separator drum.The remaining vent gas is recycled to the LORU.The liquid from the separator drum is pumped to reactor preure.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 level controller.The feed temperature to the 2nd Stage Reactor is controlled by by-paing 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，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的丁二烯和戊二烯。
Gradual lo 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 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 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89°C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 used 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 pentadiene 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 with hydrogen on flow-ratio control is heated to the hydrogenation reactor temperature in a LP2 steam-heated heat exchanger and then hot mixed C4/C5’s and
hydrogen then pa upflow through the 2nd Stage SHU Reactor where the remaining butadiene is selectively hydrogenated to n-butenes and pentadienes to respective pentenes.Since the selective hydrogenation proce is exothermic, a temperature rise occurs acro the reactor.The heat of reaction is absorbed by the C4/C5 stream as it paes through the catalyst bed.The reaction product is immediately cooled in the 2nd Stage SHU Reactor Effluent Cooler and flows to the OCU Fresh/Recycle C4/C5 Surge Drum through a back preure 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 lo 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 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 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89°C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 regeneration the 1st stage SHU Reactor is temporarily run in le 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 hot 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 preure 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 sent 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 The debutanizer overhead is combined with the Mixed C4 Raffinate from the N-Butene unit(OSBL)and the recycle C4/C5’s in the OCT Fresh/Recycle C4/C5 Surge Drum.The Mixed C4s/C5’s from this drum are pumped to the OCT reaction preure and combined with Fresh and Recycle Ethylene, mixed in a static mixer to diolve the Ethylene in the liquid C4/C5, then treated in the OCT Reactor Feed Treater.The operating preure 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.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 electric heater.The treater effluent paes 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
烯烃转换装置反应器
In this section, the OCU Reactor feed is heated to the required reaction temperature, paed through the OCU Reactor and cooled prior to OCU reactor effluent fractionation.The main reactions that occur are ethylene plus 2-butene forming propylene and ethylene plus 2-pentene forming propylene 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 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 eentially 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 Cooling 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 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 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 preure 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 gas stream containing Hydrogen, Methane, and Ethylene flows from the reflux drum on flow control to the LORU for recovery.10
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-24°C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 tower 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 preure to supply Recycle Ethylene, and a portion pumped separately to supply tower reflux on flow control.The 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 bypaes the feed chiller on temperature control, in order to maintain the OCU Reactor feed in the liquid phase at the outlet of the OCU Reactor Feed Treater.The Recycle Ethylene stream then mixes with Fresh and Recycle C4’s/C5’s 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 the Depropylenizer on flow control, reset by level control.A temperature
controller is used to control the reboiler steam to maintain the proper bottoms specification.脱乙烯塔内物料通过LP2蒸汽进行重沸，塔底产品按照液位控制器设定值以流量控制方式流入脱丙烯塔。通过温度控制器对重沸器蒸汽流量进行控制，以确保塔底产品始终符合规格要求。
1.2.8 Depropylenizer
脱丙烯塔
The Depropylenizer separates the Deethylenizer bottoms into three products: 脱丙烯塔（299-T-3302）将脱乙烯塔塔底物料分离为三种产品： • Polymer Grade Propylene(overhead)聚合物级丙烯（塔顶产品）； • C4/C5 Recycle(side-draw)C4、C5循环物流（侧线抽出）； • C4+ byproduct(bottoms product)C4+副产品（塔底产品）The tower preure is selected to condense the overhead against Cooling Water and reboil against LP2 Steam.The tower C4/C5 side-draw is cooled in a Cooling Water heat exchanger and recycled on flow control to mix with the Fresh C4/C5 feed in the OCT Fresh/Recycle C4/C5 Surge Drum.脱丙烯塔设计压力能够通过采用冷却水对塔顶产品进行冷凝，然后使用LP2蒸汽进行重沸。脱丙烯塔C4、C5侧线抽出物流通过冷却水换热器进行冷却，然后以流量控制方式循环回OCT新鲜/循环C4、C5缓冲罐，并与新鲜C4、C5进料混合。
The tower overhead is completely condensed and sent to the Depropylenizer Reflux Drum.The liquid from this drum is then pumped and split with a portion providing reflux, on flow control for the tower.The remainder of the liquid is the Polymer Grade Propylene Product and is sent to OSBL on flow control reset by level control.脱丙烯塔塔顶产品经完全冷凝后，送入脱丙烯塔回流罐。然后，将脱丙烯塔回流罐中的液体泵出并分为两股物流：一股液体以流量控制方式送
回脱丙烯塔作为回流，剩余液体作为聚合物级丙烯产品按照液位控制器设定值以流量控制方式送至界区外（OSBL）。
The tower bottoms product is C4+ by-product.It is cooled against cooling water and sent on flow control reset by level control to OSBL.脱丙烯塔塔底产品为C4副产品。该副产品按照液位控制器设定值以流量控制方式送至OSBL。
A temperature controller is used to control the reboiler steam rate to the Depropylenizer.通过温度控制器对自重沸器去脱丙烯塔的蒸汽流量进行控制。1.2.9 Regeneration System 再生系统
A treater Regeneration System is used to provide hot Regeneration Gas during the heating stage of regeneration and cold Regeneration Gas during the cooling stage of regeneration.处理器再生系统用于为每一再生加热阶段提供高温再生气以及为再生冷却阶段提供低温再生气。
1.2.9.1 Treater Regeneration 处理器再生
Hot nitrogen is supplied from the Regeneration Gas System to regenerate the OCU Reactor Feed Treaters.The Regeneration Nitrogen is supplied at the battery limits.Cold Regeneration Nitrogen is sent as cold Regeneration Nitrogen to treater when required.Hot Regeneration Nitrogen is first heated against HP steam in the Treater Regeneration Gas Steam Heater and further heated in the Treater Regeneration(electric)Gas Heater before flowing to the treater when required.由再生气系统提供热氮气，OCU反应器进料处理器进行再生。自界区提供再生氮气。低温再生氮气当需要时提供给OCU反应器进料处理器用作低温再生氮气。当要求向处理器引入高温再生氮气之前，应先通过处理器再生气体（电）加热器对高温再生氮气进行进一步加热。
The relative amounts of hot and cold Regeneration Nitrogen flow and temperature are controlled automatically to achieve complete regenerations within the required cycle times.Although the treaters are typically designed for a 48 hour adsorption cycle, they are typically designed for a 24 to 36 hour regeneration cycle.高温和低温再生氮气相对流量和温度采用自动控制方式，以确保在规定的再生周期内实现完全催化剂再生。尽管处理器吸附周期通常设计为48小时，但其再生周期通常设计为24到36小时。
Spent Regeneration Nitrogen returning from the treaters is cooled and sent to the Flare System.来自处理器的废再生氮气经冷却后送入火炬系统。1.2.9.2 C4/C5 Stripping System
C4/C5汽提系统
This system is a closed–loop proce where the preure is dependent on condensing C4’s/C5’s against Cooling Water.The system includes a C4/C5 Stripping Holding Drum, which is inventoried from the cooled 2nd Stage SHU Reactor effluent stream.Filling is controlled so that the rate is le than 5% of the forward flow from the 2nd Stage SHU Reactor effluent to avoid disturbing the OCU operation.In the first stage of regeneration, the butenes are pumped to sufficient preure, vaporized in a LP2 Steam heater and superheated to about 120℃.The hot C4/C5 vapor is then sent to the OCU Reactor Feed Treaters on flow control where it strips the C4’s/C5’s trapped on the adsorbent pores(stripping/warm soak).The effluent vapor is then condensed in the C4/C5 Stripping Condenser against Cooling Water and collected in the C4/C5 Stripping Holding Drum.Preure control on the C4/C5 Stripping Holding Drum allows for venting of non-condensables during this stripping/warm soak step.14
丁烯汽提系统为密闭回路系统，运行压力取决于通过冷却水对C4/C5 进行的冷凝。丁烯汽提系统包括一个C4/C5 汽提储罐，用于存储来自第二段SHU反应器的已冷却流出物。对去C4/C5 汽提储罐的进料流量进行控制，确保低于来自第二段SHU反应器流出物流量的5%，以避免影响OCU装置的正常运行。在第一阶段再生期间，通过泵将丁烯压力提升至足够高后经由LP2蒸汽加热器进行汽化，再过热至120℃。然后，以流量控制方式将C4/C5气体送入OCU反应器进料处理器，以将截留在吸附剂空隙中的C4/C5 汽提出来（汽提/温热浸泡）。汽提后的丁烯气体通过C4/C5 汽提冷凝器使用冷却水冷凝后收集至C4/C5 汽提储罐。对C4/C5 汽提储罐进行压力控制有助于在汽提/温热浸泡期间将不冷凝气排放出来。
When the stripping step is complete, the spent butenes/C5’s in the C4/C5 Stripping Holding Drum are drained by pumping on flow control to the drain drum of the regenerating treater.当完成汽提操作后，通过泵以流量控制方式将C4/C5汽提储罐中的废丁烯排入再生处理器排液罐。
