WO2021237483A1 - 一种丙烷脱氢装置与乙烯装置联产的工艺方法及系统 - Google Patents

一种丙烷脱氢装置与乙烯装置联产的工艺方法及系统 Download PDF

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WO2021237483A1
WO2021237483A1 PCT/CN2020/092435 CN2020092435W WO2021237483A1 WO 2021237483 A1 WO2021237483 A1 WO 2021237483A1 CN 2020092435 W CN2020092435 W CN 2020092435W WO 2021237483 A1 WO2021237483 A1 WO 2021237483A1
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crude
gas
ethanizer
rich gas
outlet
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French (fr)
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姜浩
张锦红
张军
马利峰
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Jiangsu Bosong Chemical Technology Co Ltd
Shanghai Supezet Engineering Technology Corp Ltd
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Jiangsu Bosong Chemical Technology Co Ltd
Shanghai Supezet Engineering Technology Corp Ltd
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
    • C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
    • 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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  • the invention belongs to the technical field of propane dehydrogenation and ethylene, in particular to a process method and system for co-production of an ethylene device of a propane dehydrogenation device.
  • Ethylene and propylene are important petrochemical monomers that can be used to produce a variety of polymers and intermediates. As the market demand for these products increases, so does the demand for ethylene and propylene. Ethylene plant and propane dehydrogenation plant are currently the main production methods.
  • the dry gas at the top of the propane dehydrogenation unit of the propane dehydrogenation unit contains a part of ethylene. Ethane is generally sent to the propane dehydrogenation unit with the dry gas as fuel gas to be burned. This part of ethylene, ethane is wasted, adding value Low, if the ethane in the dry gas is separated in the propane dehydrogenation unit alone, the ethylene will increase equipment investment but the income will be limited.
  • the purpose of the present invention is to provide a process method and system for co-production of a propane dehydrogenation unit and an ethylene unit, so as to solve the dry gas separation problem of the existing propane dehydrogenation unit.
  • a process method for co-production of a propane dehydrogenation unit and an ethylene unit includes the following steps:
  • the PDH product rich gas from the propane dehydrogenation reaction unit is sent to the oil and gas washing tower, and the PDH product rich gas is washed by the oil and gas washing tower and then discharged from the top of the oil and gas washing tower;
  • the PDH product rich gas discharged from the top of the oil and gas washing tower enters the rich gas compressor, and is pressurized by the rich gas compressor and sent to the outlet cooler of the rich gas compressor;
  • the PDH product rich gas cooled by the outlet cooler of the rich gas compressor is sent to the steam-water separation tank to separate the oily wastewater, and the PDH product rich gas after the steam-water separation is discharged from the top of the steam-water separation tank and sent to the rich Gas dryer
  • the PDH product rich gas is sent to the cold box after removing the remaining moisture, and is sent to the gas-liquid separation tank after further cooling;
  • the light hydrocarbon gas contained in the rich gas of the PDH product is sent from the top of the gas-liquid separation tank to the upper part of the crude deethanizer, and the first light hydrocarbon condensate at the bottom of the gas-liquid separation tank passes The condensate is pumped to the lower part of the crude de-ethanizer;
  • the light hydrocarbon gas is sent from the top of the crude de-ethanizer to the condenser of the crude de-ethanizer, and then enters the crude de-ethanizer reflux tank after being condensed by the crude de-ethanizer, where the light hydrocarbons are condensed
  • the liquid is used as the reflux liquid from the top of the crude de-ethanizer to be transported back to the top of the crude de-ethanizer by the crude de-ethanizer reflux pump. Entrance of the four-stage pyrolysis gas compressor;
  • the light hydrocarbons extracted from the bottom of the crude de-ethanizer are sent to the propylene rectification tower by the transport pump at the bottom of the crude de-ethanizer.
  • the top of the propylene rectification tower produces polymerized propylene products, and the bottom of the propylene rectification tower
  • the propane is returned to the propane dehydrogenation reaction unit as recycled propane.
  • the process method further includes: using the rectification tower system of the ethylene plant to send the dry gas of the propane dehydrogenation and the ethylene cracking gas to the rectification system of the ethylene plant for separation.
  • the theoretical plate number of the oil-gas washing tower is 4, the operating pressure is normal pressure, the temperature produced at the top of the tower is 42°C, and the temperature produced at the bottom of the tower is 55°C;
  • the outlet pressure is 1.15 MPaG; the hot end outlet temperature of the rich gas compressor cooler is 40°C.
  • the operating pressure of the steam-water separator tank is 1.1 MPaG, and the operating temperature is 40°C; the operating pressure of the rich gas dryer is 1.05 MPaG, and the operating temperature is 40°C; the inlet temperature of the rich gas end of the cold box is 40°C, The outlet temperature is -33°C, the operating pressure of the gas-liquid separation tank is 0.9MPaG, and the operating temperature is -33°C.
  • the number of theoretical plates of the crude deethanizer is 48, the operating pressure is 0.75MPaG, the temperature at the top of the tower is -23°C, and the temperature at the bottom of the tower is 18°C; the number of theoretical plates of the propylene rectification tower is 200, The operating pressure is 0.8MPaG, the temperature at the top of the tower is 15°C, and the temperature at the bottom of the tower is 27°C.
  • the rich gas composition of the PDH product is as follows: a hydrogen content of 1.57 wt%, a methane content of 0.86 wt%, an ethylene content of 0.49 wt%, an ethane content of 0.84 wt%, a propyne content of 0.01 wt%, and a propylene content of 32.11 wt%,
  • the content of propane is 62.65wt%, and the heavy component impurities are 0.95wt%.
  • composition of the dry gas extracted from the top of the reflux tank at the top of the crude deethanization tower is: hydrogen content 24.04wt%, methane content 27.34wt%, ethylene content 7.5wt%, ethane content 12.76wt%, propylene content 22.59wt% , Propane content is 5.77wt%.
  • the propylene content is 99.6% by weight, and the propane content is 0.4% by weight.
  • a system for the co-production of a propane dehydrogenation unit and an ethylene unit which is used in the process method for the co-production of any one of the above-mentioned propane dehydrogenation units and an ethylene unit, comprising:
  • Oil and gas washing tower rich gas compressor, rich gas compressor outlet cooler, steam-water separator, rich gas dryer, cold box, gas-liquid separation tank, condensate transfer pump, crude de-ethanizer, crude de-ethanizer Top condenser, top reflux tank of crude de-ethanizer, top reflux pump of crude de-ethanizer, bottom transfer pump of crude de-ethanizer, and propylene distillation tower;
  • the PDH product rich gas of the propane dehydrogenation reaction unit is connected from the rich gas outlet of the waste heat recovery equipment to the air inlet on the lower side of the oil and gas washing tower through a pipeline, and the washing water is connected to the water inlet on the upper side of the oil and gas washing tower through the pipeline;
  • the gas outlet at the top of the oil-gas washing tower is connected to the inlet of the rich gas compressor through a pipeline, and the outlet of the rich gas compressor is connected to the hot end inlet of the outlet cooler of the rich gas compressor through a pipeline;
  • the hot end outlet of the rich gas compressor outlet cooler is connected to the inlet of the steam-water separator tank through a pipe, the gas-phase outlet on the top of the steam-water separator tank is connected to the inlet of the rich gas dryer through a pipe, and the outlet of the rich gas dryer is connected to the cold box through a pipe.
  • the inlet of the rich gas end is connected, and the outlet of the rich gas end of the cold box is connected to the inlet of the gas-liquid separator through a pipe;
  • the gas-liquid outlet at the top of the gas-liquid separation tank is connected to the air inlet on the upper part of the crude de-ethanizer through a pipeline, the liquid phase outlet at the bottom of the gas-liquid separation tank is connected to the inlet of the condensate transfer pump through a pipeline, and the outlet of the condensate transfer pump passes through
  • the pipeline is connected with the liquid inlet in the middle of the crude de-ethanizer;
  • the gas phase outlet at the top of the crude de-ethanizer is connected to the hot end inlet of the crude de-ethanizer top condenser through a pipeline, and the hot outlet of the crude de-ethanizer top condenser is connected to the inlet of the crude de-ethanizer top reflux tank;
  • the gas-phase outlet at the top of the crude de-ethanizer reflux tank is connected to the inlet of the fourth stage compressor of the ethylene plant through a pipeline; the liquid-phase outlet at the bottom of the crude de-ethanizer reflux tank and the inlet of the reflux pump at the top of the crude de-ethanizer Connection, the outlet of the reflux pump at the top of the crude de-ethanizer is connected to the reflux port at the top of the crude de-ethanizer;
  • the liquid phase outlet at the bottom of the crude de-ethanizer is connected to the inlet of the crude de-ethanizer bottom transfer pump, and the outlet of the crude de-ethanizer bottom transfer pump is connected to the inlet of the propylene rectification tower;
  • the propane product outlet at the top of the propylene rectification tower is connected to the inlet of the cryogenic unit through a pipeline, and the propane outlet at the bottom of the propylene rectification tower is connected to the inlet of the reaction unit for propane dehydrogenation.
  • the process method for co-production of the propane dehydrogenation unit and the ethylene unit of the present invention uses the separation system of the ethylene unit to separate ethylene and ethane from the dry gas of the propane dehydrogenation unit, which increases the added value of the product and improves the profit.
  • the process method of the co-production of the propane dehydrogenation device and the ethylene device of the present invention shares the public engineering system and the refrigeration system, reducing equipment investment and land occupation.
  • Figure 1 is a process flow diagram of the co-production of the propane dehydrogenation unit and the ethylene unit of the present invention.
  • connection should be understood in a broad sense.
  • it can be a fixed connection or an optional connection.
  • Detachable connection, or integral connection it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • connection can be a fixed connection or an optional connection.
  • Detachable connection, or integral connection it can be a mechanical connection or an electrical connection; it can be directly connected or indirectly connected through an intermediate medium, and it can be the internal communication between two components.
  • the present application provides a process for co-production of a propane dehydrogenation unit and an ethylene unit.
  • the PDH product rich gas produced in the propane dehydrogenation reaction unit is sent to the lower side of the oil and gas washing tower 1.
  • the composition of the rich gas of the PDH product produced in the reaction unit is hydrogen content of 1.57% by weight, methane content of 0.86% by weight, ethylene content of 0.49% by weight, ethane content of 0.84% by weight, and propyne content of 0.01% by weight.
  • the propylene content is 32.11wt%
  • the propane content is 62.65wt%
  • the heavy component impurities are 0.95wt%.
  • the working parameters of the oil-gas washing tower are selected as the tower top operating temperature at 42°C, the operating pressure at normal pressure, and the tower bottom temperature at 55°C.
  • the rich gas of the PDH product is discharged from the top of the oil-gas washing tower, and the oily sewage at the bottom of the oil-gas washing tower enters the recovery or treatment system.
  • the PDH product rich gas from the oil and gas washing tower is sent to the rich gas compressor 2, and the PDH product rich gas is pressurized to 1.15MPaG and then sent to the rich gas compressor outlet cooler 3.
  • the PDH product rich gas is sent to the rich gas compressor
  • the outlet cooler is cooled to about 40°C and sent to the steam-water separation tank 4 to separate oily sewage.
  • the working parameters of the steam-water separation tank are operating pressure of 1.1 MPaG and operating temperature of 40°C.
  • the rich gas of PDH product is discharged from the top of the steam-water separation tank and sent to the rich gas dryer 5.
  • the working parameters of the rich gas dryer are the operating pressure of 1.05MPaG and the operating temperature of 40°C.
  • the rich gas of the PDH product passes through the rich gas dryer to remove the remaining After the water enters the cold box 6, it is further cooled to -33°C and then sent to the gas-liquid separation tank 7.
  • the working parameters of the gas-liquid separation tank are operating pressure 0.9MpaG and operating temperature -33°C.
  • the light hydrocarbon gas separated from the gas-liquid separation tank is discharged from the top of the gas-liquid separation tank and sent to the upper part of the crude de-ethanizer 9.
  • the first light hydrocarbon condensate at the bottom of the gas-liquid separation tank is passed through the condensate pump 8 is sent to the lower part of the crude de-ethanizer.
  • the crude de-ethanizer has a working parameter of 0.75MpaG, a top temperature of -23°C, and a bottom temperature of 18°C.
  • the light hydrocarbon gas is sent through the top of the crude deethanizer to the condenser 10 at the top of the crude deethanizer to be condensed and then enters the crude deethanizer reflux tank 11, and the second light hydrocarbon condensate in the crude deethanizer reflux tank is used as the crude
  • the reflux liquid from the top of the de-ethanizer is sent back to the top of the crude de-ethanizer by the crude de-ethanizer top reflux pump 12, and the dry gas in the crude de-ethanizer reflux tank is extracted from the top of the tank and sent to the fourth part of the ethylene plant.
  • the composition of the dry gas produced at the top of the reflux tank at the top of the crude de-ethanizer is: hydrogen content 24.04wt%, methane content 27.34wt%, ethylene content 7.5wt%, ethane The content is 12.76wt%, the propylene content is 22.59wt%, and the propane content is 5.77wt%.
  • the light hydrocarbons produced at the bottom of the crude de-ethanizer are sent to the propylene rectification tower 14 by the delivery pump 13 at the bottom of the crude de-ethanizer.
  • the operating pressure is 0.8MpaG
  • the top temperature is 15°C
  • the bottom temperature is 27°C.
  • the polymerization-grade propylene product is produced at the top of the rectification tower, and the propane produced at the bottom of the tower is returned to the reaction unit as circulating propane.
  • This application also includes systems for the co-production process of the above-mentioned propane dehydrogenation unit and ethylene unit, including oil-gas washing tower, rich gas compressor, rich gas compressor outlet cooler, steam water separator, rich gas dryer, and cold box , Gas-liquid separation tank, condensate transfer pump, crude de-ethanizer, crude de-ethanizer top condenser, crude de-ethanizer top reflux tank, crude de-ethanizer top reflux pump, crude deethanizer bottom Delivery pump and propylene distillation tower.
  • oil-gas washing tower rich gas compressor, rich gas compressor outlet cooler, steam water separator, rich gas dryer, and cold box
  • Gas-liquid separation tank condensate transfer pump
  • crude de-ethanizer crude de-ethanizer top condenser
  • crude de-ethanizer top reflux tank crude de-ethanizer top reflux pump
  • crude deethanizer bottom Delivery pump crude deethanizer bottom Delivery pump and propylene distillation tower.
  • the PDH product rich gas of the propane dehydrogenation reaction unit is connected from the rich gas outlet of the waste heat recovery equipment to the air inlet on the lower side of the oil and gas washing tower through a pipeline, and the washing water is connected to the water inlet on the upper side of the oil and gas washing tower through the pipeline;
  • the top gas outlet of the oil-gas washing tower is connected with the inlet of the rich gas compressor through a pipeline, and the outlet of the rich gas compressor is connected with the hot end inlet of the outlet cooler of the rich gas compressor through a pipeline.
  • the hot end outlet of the rich gas compressor outlet cooler is connected to the inlet of the steam-water separator tank through a pipe, the gas-phase outlet on the top of the steam-water separator tank is connected to the inlet of the rich gas dryer through a pipe, and the outlet of the rich gas dryer is connected to the cold box through a pipe.
  • the rich gas end inlet is connected, and the rich gas end outlet of the cold box is connected to the inlet of the gas-liquid separator through a pipe.
  • the gas-liquid outlet at the top of the gas-liquid separation tank is connected to the air inlet on the upper part of the crude de-ethanizer through a pipeline, the liquid phase outlet at the bottom of the gas-liquid separation tank is connected to the inlet of the condensate transfer pump through a pipeline, and the outlet of the condensate transfer pump passes through
  • the pipeline is connected with the liquid inlet in the middle of the crude de-ethanizer.
  • the gas phase outlet at the top of the crude de-ethanizer is connected to the hot end inlet of the crude de-ethanizer top condenser through a pipeline, and the hot outlet of the crude de-ethanizer top condenser is connected to the inlet of the crude deethanizer top reflux tank.
  • the gas-phase outlet at the top of the crude de-ethanizer reflux tank is connected to the inlet of the fourth stage compressor of the ethylene plant through a pipeline; the liquid-phase outlet at the bottom of the crude de-ethanizer reflux tank and the inlet of the reflux pump at the top of the crude de-ethanizer Connect, the outlet of the reflux pump at the top of the crude de-ethanizer is connected with the reflux port at the top of the crude de-ethanizer.
  • the liquid phase outlet at the bottom of the crude de-ethanizer is connected to the inlet of the crude de-ethanizer bottom transfer pump, and the outlet of the crude de-ethanizer bottom transfer pump is connected to the inlet of the propylene rectification tower.
  • the propane product outlet at the top of the propylene rectification tower is connected to the inlet of the cryogenic unit through a pipeline, and the propane outlet at the bottom of the propylene rectification tower is connected to the inlet of the reaction unit for propane dehydrogenation.

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Abstract

一种丙烷脱氢装置与乙烯装置联产的工艺方法及系统，包括油气水洗塔（1）、富气压缩机（2）、富气压缩机出口冷却器（3）、汽水分离器（4）、富气干燥器（5）、冷箱（6）、气液分离罐（7）、凝液输送泵（8）、粗脱乙烷塔（9）、粗脱乙烷塔顶冷凝器（10）、粗脱乙烷塔顶回流罐（11）、粗脱乙烷塔顶回流泵（12）、粗脱乙烷塔底输送泵（13）及丙烯精馏塔（14）。

Description

一种丙烷脱氢装置与乙烯装置联产的工艺方法及系统 技术领域
本发明属于丙烷脱氢与乙烯技术领域，特别是指一种丙烷脱氢装置乙烯装置联产的工艺方法及系统。
背景技术
乙烯和丙烯是一种重要的石油化学品单体，可用于生产多种聚合物和中间体。随着这些产品市场需求的增加，乙烯和丙烯的需求量也增加。乙烯装置和丙烷脱氢装置是目前主要的制备方法。
丙烷脱氢装置脱丙烷塔顶的干气中含有一部分乙烯，乙烷一般都是随着干气作为燃料气送至丙烷脱氢装置烧掉，这部分乙烯，乙烷就浪费掉了，附加值低，如果单独在丙烷脱氢装置内分离干气中的乙烷，乙烯增加设备投资但获得的收益有限。
针对上述问题，如何通过工艺技术方案的改变来实现乙烯装置与丙烷脱氢装置的联产，回收丙烷脱氢干气中的这部分丙烯、丙烷，成为亟需解决的问题。
发明内容
本发明的目的是提供一种丙烷脱氢装置与乙烯装置联产的工艺方法及系统，以解决现有丙烷脱氢装置的干气分离问题。
本发明是通过以下技术方案实现的：
一种丙烷脱氢装置与乙烯装置联产的工艺方法，包括以下步骤：
S1、来自丙烷脱氢反应单元的PDH产品富气送至油气水洗塔，PDH产品富气经过油气水洗塔洗涤后从油气水洗塔的塔顶排出；
S2、从油气水洗塔的塔顶排出的PDH产品富气进入富气压缩机，经过富气压缩机增压后送至富气压缩机出口冷却器；
S3、经过富气压缩机出口冷却器冷却后的PDH产品富气送至汽水分离罐分离出今油污水，经过汽水分离后的PDH产品富气从所述汽水分离罐的顶部排出后送至富气干燥器；
S4、在所述富气干燥器内，PDH产品富气脱除剩余水分后被送至冷箱，经过进一步冷却后被送至气液分离罐；
S5、在气液分离罐内，PDH产品富气中所包含的轻烃气体从气液分离罐的顶部送至粗脱乙烷塔的上部，气液分离罐底部的第一轻烃凝液通过凝液泵送至所述粗脱乙烷塔的下部；
S6、轻烃气体从所述粗脱乙烷塔顶被送至粗脱乙烷塔顶冷凝器，经过粗脱乙烷塔顶冷凝器冷凝后进入粗脱乙烷回流罐，其中的轻烃凝液作为粗脱乙烷塔顶回流液通过粗脱乙烷塔顶回流泵输送回所述粗脱乙烷塔顶部，其中的干气从粗脱乙烷回流罐采出后送至乙烯装置的第四段裂解气压缩机入口；
S7、从粗脱乙烷塔底采出的轻烃通过粗脱乙烷塔底输送泵送至丙烯精馏塔，丙烯精馏塔顶采出聚合级的丙烯产品，丙烯精馏塔底采出的丙烷作为循环丙烷返回丙烷脱氢反应单元。
进一步的，所述工艺方法还包括：利用乙烯装置的精馏塔系统，将丙烷脱氢的干气与乙烯裂解气一同送至乙烯装置的精馏系统进行分离。
进一步的，所述油气水洗塔的理论塔板数为4层，操作压力为常压，其塔顶采出的温度为42℃，塔底采出温度为55℃；所述富气压缩机的出口压力为1.15MPaG；所述富气压缩机冷却器的热端出口温度为40℃。
进一步的，所述汽水分离罐的操作压力为1.1MPaG，操作温度为40℃；所述富气干燥器的操作压力为1.05MPaG，操作温度40℃；冷箱的富气端进口温度40℃，出口温度-33℃，所述气液分离罐的操作压力0.9MPaG，操温度-33℃。
进一步的，所述粗脱乙烷塔理论板数为48块，操作压力为0.75MPaG，塔顶温度为-23℃，塔底温度为18℃；所述丙烯精馏塔理论板数为200，操作压力为0.8MPaG，塔顶温度为15℃，塔底温度为27℃。
进一步的，所述PDH产品富气组成为：氢气含量1.57wt％，甲烷含量0.86wt％，乙烯含量0.49wt％，乙烷含量0.84wt％，丙炔含量0.01wt％， 丙烯含量32.11wt％，丙烷含量62.65wt％，重组分杂质0.95wt％。
进一步的，粗脱乙烷塔顶回流罐顶部采出的干气组成为：氢气含量24.04wt％，甲烷含量27.34wt％，乙烯含量7.5wt％，乙烷含量12.76wt％，丙烯含量22.59wt％，丙烷含量5.77wt％。
进一步的，丙烯精馏塔顶采出的丙烯产品中丙烯含量99.6wt％，丙烷含量0.4wt％。
一种丙烷脱氢装置与乙烯装置联产的系统，用于上述任一项的丙烷脱氢装置与乙烯装置联产的工艺方法，包括：
油气水洗塔、富气压缩机、富气压缩机出口冷却器、汽水分离器、富气干燥器、冷箱、气液分离罐、凝液输送泵、粗脱乙烷塔、粗脱乙烷塔顶冷凝器、粗脱乙烷塔顶回流罐、粗脱乙烷塔顶回流泵、粗脱乙烷塔底输送泵及丙烯精馏塔；
丙烷脱氢反应单元的PDH产品富气从余热回收设备富气出口通过管道与油气水洗塔的侧下部的进气口连接，洗涤水通过管道与油气水洗塔的侧上部的进水口连接；所述油气水洗塔的顶部出气口通过管道与富气压缩机的入口连接，富气压缩机的出口与富气压缩机出口冷却器的热端的进口通过管道连接；
富气压缩机出口冷却器的热端的出口通过管道与汽水分离罐的进口相连，汽水分离罐顶部气相出口通过管道与富气干燥器的进口相连，富气干燥器的出口通过管道与冷箱的富气端进口连接，冷箱的富气端出口通过管道与气液分离器的进口相连；
气液分离罐顶部的气相出口通过管道与粗脱乙烷塔上部的进气口连接，气流分离罐底部的液相出口通过管路与凝液输送泵的进口连接，凝液输送泵的出口通过管道与粗脱乙烷塔的中部进液口连接；
粗脱乙烷塔顶部的气相出口通过管道与粗脱乙烷塔顶冷凝器的热端进口连接，粗脱乙烷塔顶冷凝器热出口与粗脱乙烷塔顶回流罐进口连接；
粗脱乙烷塔顶回流罐顶部的气相出口通过管道连接到乙烯装置的第四段压缩机入口；粗脱乙烷塔顶回流罐底部的液相出口与粗脱乙烷塔顶回流泵的入口连接，粗脱乙烷塔顶回流泵的出口与粗脱乙烷塔顶回流口相连；
粗脱乙烷塔底的液相出口与粗脱乙烷塔底输送泵的入口连接，粗脱乙烷 塔底输送泵的出口与丙烯精馏塔的进口连接；
丙烯精馏塔顶的丙烷产品出口通过管道与深冷单元的入口连接，丙烯精馏塔底的丙烷出口与丙烷脱氢的反应单元入口连接。
本发明的有益效果是：
1、本发明的丙烷脱氢装置与乙烯装置联产的工艺方法，利用乙烯装置的分离系统分离丙烷脱氢装置干气中的乙烯，乙烷，增加了产品附加值，提高了收益。
2、本发明的丙烷脱氢装置与乙烯装置联产的工艺方法，共用公用工程系统和制冷系统，减少了设备投资和占地。
附图说明
图1为本发明丙烷脱氢装置、乙烯装置联产的工艺流程图。
附图标记说明
1-油气水洗塔；2-富气压缩机；3-富气压缩机出口冷却器；4-汽水分离罐；5-富气干燥器；6-冷箱；7-气液分离罐；8-凝液输送泵；9-粗脱乙烷塔；10-粗脱乙烷塔顶冷凝器；11-粗脱乙烷塔顶回流罐；12-粗脱乙烷塔顶回流泵；13-粗脱乙烷塔底输送泵；14-丙烯精馏塔。
具体实施方式
需要说明的是，在不冲突的情况下，本发明创造中的实施例及实施例中的特征可以相互组合。
在本发明创造的描述中，需要理解的是，术语“上”、“下”、“顶”、“底”等指示的方位或位置关系为基于附图所示的方位或位置关系，仅是为了便于描述本发明创造和简化描述，而不是指示或暗示所指的装置或元件必须具有特定的方位、以特定的方位构造和操作，因此不能理解为对本发明创造的限制。此外，术语“第一”、“第二”等仅用于描述目的，而不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量。由此，限定有“第一”、“第二”等的特征可以明示或者隐含地包括一个或者更多个该特征。在本发明创造的描述中，除非另有说明，“多个”的含义是两个或两个以上。
在本发明创造的描述中，需要说明的是，除非另有明确的规定和限定，术语“安装”、“相连”、“连接”应做广义理解，例如，可以是固定连接，也可以是可拆卸连接，或一体地连接；可以是机械连接，也可以是电连接；可以是直接相连，也可以通过中间媒介间接相连，可以是两个元件内部的连通。对于本领域的普通技术人员而言，可以通过具体情况理解上述术语在本发明创造中的具体含义。
下面将参考附图并结合实施例来详细说明本发明创造。
如图1所示，本申请提供一种丙烷脱氢装置与乙烯装置联产的工艺，首先在丙烷脱氢反应单元产生的PDH产品富气送至油气水洗塔1的侧下部。
在本实施例中，在反应单元所生产的PDH产品富气的组成为氢气含量1.57wt％，甲烷含量0.86wt％，乙烯含量0.49wt％，乙烷含量0.84wt％，丙炔含量0.01wt％，丙烯含量32.11wt％，丙烷含量62.65wt％，重组分杂质0.95wt％。
在本实施例中，油气水洗塔的工作参数选为塔顶操作温度为42℃、操作压力为常压、塔底温度为55℃。PDH产品富气经过油气水洗塔的洗涤后从油气水洗塔的塔顶排出，油气水洗塔的塔底的含油污水进入回收或处理系统。
从油气水洗塔出来的PDH产品富气被送至富气压缩机2，将PDH产品富气增压到1.15MPaG后送至富气压缩机出口冷却器3，PDH产品富气被富气压缩机出口冷却器冷却到40℃左右，送至汽水分离罐4分离出含油污水，在本实施例中，汽水分离罐的工作参数为操作压力为1.1MPaG，操作温度40℃。
PDH产品富气从汽水分离罐顶部排出并送至富气干燥器5，富气干燥器的工作参数为操作压力为1.05MPaG，操作温度40℃，PDH产品富气经过富气干燥器脱除剩余水分后进入冷箱6，在进一步冷却到-33℃后被送至气液分离罐7，在本实施例中，气液分离罐的工作参数为操作压力0.9MpaG，操温度-33℃。
从气液分离罐中分离出的轻烃气体从气液分离罐的顶部排出后被送至粗脱乙烷塔9的上部，气液分离罐的底部的第一轻烃凝液通过凝液泵8被送至粗脱乙烷塔的下部，在本实施例中，粗脱乙烷塔的工作参数为0.75MpaG， 塔顶温度为-23℃，塔底温度为18℃。
轻烃气体通过粗脱乙烷塔顶送至粗脱乙烷塔顶冷凝器10冷凝后进入粗脱乙烷塔回流罐11，粗脱乙烷塔回流罐中的第二轻烃凝液作为粗脱乙烷塔顶回流液通过粗脱乙烷塔顶回流泵12输送回粗脱乙烷塔的顶部，粗脱乙烷塔回流罐中的干气从罐顶采出送至乙烯装置的第四段裂解气压缩机入口，在本实施例中，粗脱乙烷塔顶回流罐顶部采出的干气组成为：氢气含量24.04wt％，甲烷含量27.34wt％，乙烯含量7.5wt％，乙烷含量12.76wt％，丙烯含量22.59wt％，丙烷含量5.77wt％。
粗脱乙烷塔底采出的轻烃通过粗脱乙烷塔底输送泵13送至丙烯精馏塔14，操作压力为0.8MpaG，塔顶温度为15℃，塔底温度为27℃，丙烯精馏塔顶采出聚合级的丙烯产品，塔底采出的丙烷作为循环丙烷返回反应单元。
本申请还包括用于上述丙烷脱氢装置与乙烯装置联产的工艺的系统，包括油气水洗塔、富气压缩机、富气压缩机出口冷却器、汽水分离器、富气干燥器、冷箱、气液分离罐、凝液输送泵、粗脱乙烷塔、粗脱乙烷塔顶冷凝器、粗脱乙烷塔顶回流罐、粗脱乙烷塔顶回流泵、粗脱乙烷塔底输送泵及丙烯精馏塔。
丙烷脱氢反应单元的PDH产品富气从余热回收设备富气出口通过管道与油气水洗塔的侧下部的进气口连接，洗涤水通过管道与油气水洗塔的侧上部的进水口连接；所述油气水洗塔的顶部出气口通过管道与富气压缩机的入口连接，富气压缩机的出口与富气压缩机出口冷却器的热端的进口通过管道连接。
富气压缩机出口冷却器的热端的出口通过管道与汽水分离罐的进口相连，汽水分离罐顶部气相出口通过管道与富气干燥器的进口相连，富气干燥器的出口通过管道与冷箱的富气端进口连接，冷箱的富气端出口通过管道与气液分离器的进口相连。
气液分离罐顶部的气相出口通过管道与粗脱乙烷塔上部的进气口连接，气流分离罐底部的液相出口通过管路与凝液输送泵的进口连接，凝液输送泵的出口通过管道与粗脱乙烷塔的中部进液口连接。
粗脱乙烷塔顶部的气相出口通过管道与粗脱乙烷塔顶冷凝器的热端进口连接，粗脱乙烷塔顶冷凝器热出口与粗脱乙烷塔顶回流罐进口连接。
粗脱乙烷塔顶回流罐顶部的气相出口通过管道连接到乙烯装置的第四段压缩机入口；粗脱乙烷塔顶回流罐底部的液相出口与粗脱乙烷塔顶回流泵的入口连接，粗脱乙烷塔顶回流泵的出口与粗脱乙烷塔顶回流口相连。
粗脱乙烷塔底的液相出口与粗脱乙烷塔底输送泵的入口连接，粗脱乙烷塔底输送泵的出口与丙烯精馏塔的进口连接。
丙烯精馏塔顶的丙烷产品出口通过管道与深冷单元的入口连接，丙烯精馏塔底的丙烷出口与丙烷脱氢的反应单元入口连接。
本发明提出的一种丙烷脱氢装置和乙烯装置联产的工艺及系统，已通过实施例进行了描述，相关技术人员明显能在不脱离本发明的内容、精神和范围内对本文所述的产品和制作方法进行改动或适当变更与组合，来实现本发明的技术。特别需要指出的是，所有相类似的替换和改动对本领域技术人员来说是显而易见的，它们都被视为包括在本发明的精神、范围和内容。

Claims (9)

  1. 一种丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，包括以下步骤：
    S1、来自丙烷脱氢反应单元的PDH产品富气送至油气水洗塔，PDH产品富气经过油气水洗塔洗涤后从油气水洗塔的塔顶排出；
    S2、从油气水洗塔的塔顶排出的PDH产品富气进入富气压缩机，经过富气压缩机增压后送至富气压缩机出口冷却器；
    S3、经过富气压缩机出口冷却器冷却后的PDH产品富气送至汽水分离罐分离出今油污水，经过汽水分离后的PDH产品富气从所述汽水分离罐的顶部排出后送至富气干燥器；
    S4、在所述富气干燥器内，PDH产品富气脱除剩余水分后被送至冷箱，经过进一步冷却后被送至气液分离罐；
    S5、在气液分离罐内，PDH产品富气中所包含的轻烃气体从气液分离罐的顶部送至粗脱乙烷塔的上部，气液分离罐底部的第一轻烃凝液通过凝液泵送至所述粗脱乙烷塔的下部；
    S6、轻烃气体从所述粗脱乙烷塔顶被送至粗脱乙烷塔顶冷凝器，经过粗脱乙烷塔顶冷凝器冷凝后进入粗脱乙烷回流罐，其中的轻烃凝液作为粗脱乙烷塔顶回流液通过粗脱乙烷塔顶回流泵输送回所述粗脱乙烷塔顶部，其中的干气从粗脱乙烷塔回流罐采出后送至乙烯装置的第四段裂解气压缩机入口；
    S7、从粗脱乙烷塔底采出的轻烃通过粗脱乙烷塔底输送泵送至丙烯精馏塔，丙烯精馏塔顶采出聚合级的丙烯产品，丙烯精馏塔底采出的丙烷作为循环丙烷返回丙烷脱氢反应单元。
  2. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，所述工艺方法还包括：利用乙烯装置的精馏塔系统，将丙烷脱氢的干气与乙烯裂解气一同送至乙烯装置的精馏系统进行分离。
  3. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，所述油气水洗塔的理论塔板数为层，操作压力为常压，其塔顶采出的温度为42℃，塔底采出温度为55℃；所述富气压缩机的出口压力为 1.15MPaG；所述富气压缩机冷却器的热端出口温度为40℃。
  4. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，所述汽水分离罐的操作压力为1.1MPaG，操作温度为40℃；所述富气干燥器的操作压力为1.05MPaG，操作温度40℃；冷箱的富气端进口温度40℃，出口温度-33℃，所述气液分离罐的操作压力0.9MPaG，操温度-33℃。
  5. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，所述粗脱乙烷塔理论板数为48块，操作压力为0.75MPaG，塔顶温度为-23℃，塔底温度为18℃；所述丙烯精馏塔理论板数为200，操作压力为0.8MPaG，塔顶温度为15℃，塔底温度为27℃。
  6. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，所述PDH产品富气组成为：氢气含量1.57wt％，甲烷含量0.86wt％，乙烯含量0.49wt％，乙烷含量0.84wt％，丙炔含量0.01wt％，丙烯含量32.11wt％，丙烷含量62.65wt％，重组分杂质0.95wt％。
  7. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，粗脱乙烷塔顶回流罐顶部采出的干气组成为：氢气含量24.04wt％，甲烷含量27.34wt％，乙烯含量7.5wt％，乙烷含量12.76wt％，丙烯含量22.59wt％，丙烷含量5.77wt％。
  8. 根据权利要求1所述的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，丙烯精馏塔顶采出的丙烯产品中丙烯含量99.6wt％，丙烷含量0.4wt％。
  9. 一种丙烷脱氢装置与乙烯装置联产的系统，用于上述权利要求1至8中任一项的丙烷脱氢装置与乙烯装置联产的工艺方法，其特征在于，包括：
    油气水洗塔、富气压缩机、富气压缩机出口冷却器、汽水分离器、富气干燥器、冷箱、气液分离罐、凝液输送泵、粗脱乙烷塔、粗脱乙烷塔顶冷凝器、粗脱乙烷塔顶回流罐、粗脱乙烷塔顶回流泵、粗脱乙烷塔底输送泵及丙烯精馏塔；
    丙烷脱氢反应单元的PDH产品富气从余热回收设备富气出口通过管道与油气水洗塔的侧下部的进气口连接，洗涤水通过管道与油气水洗塔的侧上部的 进水口连接；所述油气水洗塔的顶部出气口通过管道与富气压缩机的入口连接，富气压缩机的出口与富气压缩机出口冷却器的热端的进口通过管道连接；
    富气压缩机出口冷却器的热端的出口通过管道与汽水分离罐的进口相连，汽水分离罐顶部气相出口通过管道与富气干燥器的进口相连，富气干燥器的出口通过管道与冷箱的富气端进口连接，冷箱的富气端出口通过管道与气液分离器的进口相连；
    气液分离罐顶部的气相出口通过管道与粗脱乙烷塔上部的进气口连接，气流分离罐底部的液相出口通过管路与凝液输送泵的进口连接，凝液输送泵的出口通过管道与粗脱乙烷塔的中部进液口连接；
    粗脱乙烷塔顶部的气相出口通过管道与粗脱乙烷塔顶冷凝器的热端进口连接，粗脱乙烷塔顶冷凝器热出口与粗脱乙烷塔顶回流罐进口连接；
    粗脱乙烷塔顶回流罐顶部的气相出口通过管道连接到乙烯装置的第四段压缩机入口；粗脱乙烷塔顶回流罐底部的液相出口与粗脱乙烷塔顶回流泵的入口连接，粗脱乙烷塔顶回流泵的出口与粗脱乙烷塔顶回流口相连；
    粗脱乙烷塔底的液相出口与粗脱乙烷塔底输送泵的入口连接，粗脱乙烷塔底输送泵的出口与丙烯精馏塔的进口连接；
    丙烯精馏塔顶的丙烷产品出口通过管道与深冷单元的入口连接，丙烯精馏塔底的丙烷出口与丙烷脱氢的反应单元入口连接。
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