CN104817421A - Method for separating light hydrocarbon by using light hydrocarbon separation device - Google Patents
Method for separating light hydrocarbon by using light hydrocarbon separation device Download PDFInfo
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Abstract
The invention relates to a method for separating light hydrocarbon by using a light hydrocarbon separation device. The method overcomes the problems of great processing difficulty and incapability of effective separation of light hydrocarbon and comprehensive utilization of separated light hydrocarbon in a conventional light hydrocarbon separation method using a conventional light hydrocarbon separation device. The method comprises the following steps: introducing stable crude light hydrocarbon into an entering-and-existing material heat exchanger for heat exchanging, controlling temperature and pressure of tower-top products in a degassing tower, and condensing the tower-top products; controlling the temperature and the pressure of tower-bottom products in the degassing tower, and allowing the tower-bottom products to undergo heat exchanging; controlling the temperature and the pressure of tower-top products in a liquefied gas separation tower, and carrying out heat exchanging, cooling and pressurizing on the tower-top products; controlling the temperature and the pressure of tower-bottom products in the liquefied gas separation tower and cooling the tower-bottom products; controlling the temperature and the pressure of tower-top products in a product separation tower, cooling and pressurizing the tower-top products in a tower-top condenser, and introducing the tower-top products into a light stable light hydrocarbon cooler for cooling; and controlling the temperature and the pressure of the tower-bottom products in the product separation tower, and carrying out pressurizing and cooling. The method is used for separating light hydrocarbon with the light hydrocarbon separation device.
Description
Technical field
The present invention relates to the method that lighter hydrocarbons tripping device lighter hydrocarbons are separated.
Background technology
Lighter hydrocarbons tripping device is that the thick stable light hydrocarbon that synthesizing stable lighter hydrocarbons facilities comes is carried out rectifying separation.A part of dissolved hydrogen, CO is further comprises by from the thick stable light hydrocarbon of synthesizing stable lighter hydrocarbons facilities
2, C
1~ C
2light hydrocarbon gaseous fraction, and C
3~ C
4and C
10above heavy oil component, cannot directly utilize.
Along with Economic development, energy demand increases, and the comprehensive utilization of the energy becomes important development direction.There is the effective utilization being unfavorable for lighter hydrocarbons resource in the method that existing lighter hydrocarbons tripping device lighter hydrocarbons are separated, intractability is large, cannot effectively be separated, the problem that isolated lighter hydrocarbons can not fully utilize.
Summary of the invention
The present invention is that the method that will solve the separation of existing lighter hydrocarbons tripping device lighter hydrocarbons exists the effective utilization being unfavorable for lighter hydrocarbons resource, intractability is large, effectively cannot be separated, the problem that isolated lighter hydrocarbons can not fully utilize, and provide the method for a kind of lighter hydrocarbons tripping device lighter hydrocarbons separation.
The thick stable light hydrocarbon of the present invention to be 45 DEG C and pressure by temperature be 2.5MPa passes into the thick stable light hydrocarbon entrance end of turnover material heat exchanger, thick stable light hydrocarbon heat exchange to the temperature controlling to enter turnover material heat exchanger is 117.6 DEG C, thick stable light hydrocarbon after heat exchange passes into gas removal tower, controlling gas removal tower overhead temperature is 120 DEG C, pressure is 2.1MPa, and absorbing tower bottom product is mixed with gas removal tower overhead and passes into gas removal column overhead condenser, the mixture temperature controlled after gas removal column overhead condenser condenses is 46 DEG C, condensed mixture is passed into the gas-liquid separation of gas removal column overhead tank, isolated process water is transported to synthesizing stable lighter hydrocarbons facilities by process water discharge nozzle, isolated liquid hydrocarbon is back to gas removal column overhead by gas removal column overhead reflux pump, isolated gas-phase transport is to absorption tower,
Controlling gas removal tower bottom product temperature is 187 DEG C, pressure is 2.14MPa, gas removal tower bottom product is passed into out the gas removal tower bottom product entrance end of material heat exchanger, the gas removal tower bottom product heat exchange controlling to enter turnover material heat exchanger is 117.5 DEG C to temperature, and the gas removal tower bottom product after heat exchange is passed into liquefied gas knockout tower;
Controlling liquefied gas knockout tower overhead product temperature is 75.5 DEG C, pressure is 1.5MPa, controlling liquefied gas knockout tower overhead product by heat exchange after liquefied gas knockout tower overhead condenser is 68.5 DEG C to temperature, and the liquefied gas knockout tower overhead product after heat exchange passes into liquefied gas knockout tower backflash, obtains C
3and C
4liquid hydrocarbon, by part C
3and C
4liquid hydrocarbon is back to liquefied gas separation column, by part C
3and C
4liquid hydrocarbon is cooled to 46 DEG C by LPG water cooler, then by the part C of cooling
3and C
4liquid hydrocarbon passes into LPG surge tank and LPG product pump successively, C after the pressurization of control LPG product pump
3and C
4the pressure of liquid hydrocarbon is 1.7MPa, obtains LPG product, finally LPG product is sent into tank field by LPG product discharge pipe;
Controlling liquefied gas knockout tower bottom product temperature is 197 DEG C, pressure is 1.55MPa, partial liquefaction gas knockout tower bottom product is passed into the pressurization of lean solution feeding pump, liquefied gas knockout tower bottom product after pressurization passes into oil-poor precooler and the cooling of oil-poor water cooler successively, and controlling liquefied gas knockout tower bottom product, to be cooled to temperature be 40 DEG C, finally cooled liquefied gas knockout tower bottom product passed into absorption tower;
Another part liquefied gas knockout tower bottom product is passed into product separation tower, controlling product separation tower overhead temperature is 134 DEG C, pressure is 0.19MPa, product separation tower overhead being passed into product separation column overhead condenser, to be cooled to temperature be 74 DEG C, then cooled product separation tower overhead is passed into product separation column overhead tank and product separation column overhead reflux pump successively, control product separation column overhead reflux pump and product separation tower overhead is forced into 0.54MPa, product separation tower overhead after a part being pressurizeed again passes into product separation tower, product separation tower overhead after being pressurizeed by another part passes into light stable light hydrocarbon water cooler, and to be cooled to temperature be 45 DEG C, obtain stable light hydrocarbon product, stable light hydrocarbon product is delivered to intermediate tank farm by stable light hydrocarbon product discharge pipe,
Controlling product separation tower bottom product temperature is 221.9 DEG C, pressure is 0.23MPa, product separation tower bottom product being passed into product separation tower column bottoms pump, to be forced into pressure be 1.0MPa, then the product separation tower bottom product after pressurization is passed into successively heavy lighter hydrocarbons water cooler and heavy lighter hydrocarbons to regulate water cooler to be cooled to temperature to be 77 DEG C, finally cooled product separation tower bottom product to be delivered to tank field by weight stable light hydrocarbon product discharge pipe;
Absorption tower overhead product obtains fuel gas, and fuel gas is delivered to plant area's fuel gas pipe network by fuel gas discharge nozzle.
Advantage of the present invention: the present invention, by product separation, obtains the products such as LPG product, stable light hydrocarbon product and fuel gas respectively, can fully utilize, improve lighter hydrocarbons added value, make maximizing the benefits; Flow process and equipment is simple, turndown ratio is large, less investment, energy consumption are low, can meet various production decision, solves lighter hydrocarbons and to volatilize the safety and environmental issue brought.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of lighter hydrocarbons tripping device of the present invention.
Embodiment
Embodiment one: composition graphs 1, present embodiment is that the method steps that a kind of lighter hydrocarbons tripping device lighter hydrocarbons are separated is as follows:
The thick stable light hydrocarbon of to be 45 DEG C and pressure by temperature be 2.5MPa passes into the thick stable light hydrocarbon entrance end 1-1 of turnover material heat exchanger 1, thick stable light hydrocarbon heat exchange to the temperature controlling to enter turnover material heat exchanger 1 is 117.6 DEG C, thick stable light hydrocarbon after heat exchange passes into gas removal tower 2, controlling gas removal tower 2 overhead product temperature is 120 DEG C, pressure is 2.1MPa, and absorption tower 23 bottom product is mixed with gas removal tower 2 overhead product and passes into gas removal column overhead condenser 3, controlling the condensed mixture temperature of gas removal column overhead condenser 3 is 46 DEG C, condensed mixture is passed into the gas-liquid separation of gas removal column overhead tank 4, isolated process water is transported to synthesizing stable lighter hydrocarbons facilities by process water discharge nozzle 25, isolated liquid hydrocarbon is back to gas removal tower 2 tower top by gas removal column overhead reflux pump 5, isolated gas-phase transport is to absorption tower 23,
Controlling gas removal tower 2 bottom product temperature is 187 DEG C, pressure is 2.14MPa, gas removal tower 2 bottom product is passed into out the gas removal tower bottom product entrance end 1-3 of material heat exchanger 1, the gas removal tower 2 bottom product heat exchange controlling to enter turnover material heat exchanger 1 is 117.5 DEG C to temperature, and gas removal tower 2 bottom product after heat exchange is passed into liquefied gas knockout tower 6;
Controlling liquefied gas knockout tower 6 overhead product temperature is 75.5 DEG C, pressure is 1.5MPa, controlling liquefied gas knockout tower 6 overhead product is 68.5 DEG C by heat exchange to temperature after liquefied gas knockout tower overhead condenser 10, liquefied gas knockout tower 6 overhead product after heat exchange passes into liquefied gas knockout tower backflash 11, obtains C
3and C
4liquid hydrocarbon, by part C
3and C
4liquid hydrocarbon is back to liquefied gas knockout tower 6 top, by part C
3and C
4liquid hydrocarbon is cooled to 46 DEG C by LPG water cooler 12, then by the part C of cooling
3and C
4liquid hydrocarbon passes into LPG surge tank 13 and LPG product pump 14 successively, C after control LPG product pump 14 pressurizes
3and C
4the pressure of liquid hydrocarbon is 1.7MPa, obtains LPG product, finally LPG product is sent into tank field by LPG product discharge pipe 26;
Controlling liquefied gas knockout tower 6 bottom product temperature is 197 DEG C, pressure is 1.55MPa, partial liquefaction gas knockout tower 6 bottom product is passed into lean solution feeding pump 7 pressurize, liquefied gas knockout tower 6 bottom product after pressurization passes into oil-poor precooler 8 successively and oil-poor water cooler 9 cools, and controlling liquefied gas knockout tower 6 bottom product, to be cooled to temperature be 40 DEG C, finally cooled liquefied gas knockout tower 6 bottom product passed into absorption tower 23;
Another part liquefied gas knockout tower 6 bottom product is passed into product separation tower 15, controlling product separation tower 15 overhead product temperature is 134 DEG C, pressure is 0.19MPa, product separation tower 15 overhead product being passed into product separation column overhead condenser 16, to be cooled to temperature be 74 DEG C, then cooled product separation tower 15 overhead product is passed into product separation column overhead tank 17 and product separation column overhead reflux pump 18 successively, control product separation column overhead reflux pump 18 and product separation tower 15 overhead product is forced into 0.54MPa, product separation tower 15 overhead product after a part being pressurizeed again passes into product separation tower 15, product separation tower 15 overhead product after being pressurizeed by another part passes into light stable light hydrocarbon water cooler 19, and to be cooled to temperature be 45 DEG C, obtain stable light hydrocarbon product, stable light hydrocarbon product is delivered to intermediate tank farm by stable light hydrocarbon product discharge pipe 27,
Controlling product separation tower 15 bottom product temperature is 221.9 DEG C, pressure is 0.23MPa, product separation tower 15 bottom product being passed into product separation tower column bottoms pump 20, to be forced into pressure be 1.0MPa, then product separation tower 15 bottom product after pressurization is passed into successively heavy lighter hydrocarbons water cooler 21 and heavy lighter hydrocarbons to regulate water cooler 22 to be cooled to temperature to be 77 DEG C, finally cooled product separation tower 15 bottom product to be delivered to tank field by heavy stable light hydrocarbon product discharge pipe 28;
Absorption tower 23 overhead product obtains fuel gas, and fuel gas is delivered to plant area's fuel gas pipe network by fuel gas discharge nozzle 29.
A kind of lighter hydrocarbons tripping device described in present embodiment is by passing in and out material heat exchanger 1, gas removal tower 2, gas removal column overhead condenser 3, gas removal column overhead tank 4, gas removal column overhead reflux pump 5, liquefied gas knockout tower 6, lean solution feeding pump 7, oil-poor precooler 8, oil-poor water cooler 9, liquefied gas knockout tower overhead condenser 10, liquefied gas knockout tower backflash 11, LPG water cooler 12, LPG surge tank 13, LPG product pump 14, product separation tower 15, product separation column overhead condenser 16, product separation column overhead tank 17, product separation column overhead reflux pump 18, light stable light hydrocarbon water cooler 19, product separation tower column bottoms pump 20, heavy lighter hydrocarbons water cooler 21, heavy lighter hydrocarbons regulate water cooler 22 and absorption tower 23 to form,
Described turnover material heat exchanger 1 is provided with thick stable light hydrocarbon entrance end 1-1, thick stable light hydrocarbon exit end 1-2, gas removal tower bottom product entrance end 1-3 and gas removal tower bottoms outlet end 1-4, and thick stable light hydrocarbon entrance end 1-1 and thick stable light hydrocarbon exit end 1-2 connects, gas removal tower bottom product entrance end 1-3 and gas removal tower bottoms outlet end 1-4 connects;
Described gas removal tower 2 is provided with gas removal tower entrance end 2-1, gas removal trim the top of column mouth 2-2, gas removal column overhead exit end 2-3 and gas removal tower tower bottom outlet end 2-4;
Described liquefied gas knockout tower 6 is provided with liquefied gas knockout tower entrance end 6-1, liquefied gas is separated tower top refluxing opening 6-2, liquefied gas knockout tower tower top outlet end 6-3 and liquefied gas knockout tower tower bottom outlet end 6-4;
Described product separation tower 15 is provided with product separation tower entrance end 15-1, product separation trim the top of column mouth 15-2, product separation column overhead exit end 15-3 and product separation tower tower bottom outlet end 15-4;
Described absorption tower 23 is provided with absorption tower first entrance end 23-1, absorption tower second entrance end 23-2, absorption tower tower top outlet end 23-3 and absorbing tower bottom outlet end 23-4;
Thick stable light hydrocarbon entrance end 1-1 and thick stable light hydrocarbon feed-pipe 24 connect, and thick stable light hydrocarbon exit end 1-2 is connected by connecting pipe and gas removal tower entrance end 2-1;
Gas removal tower tower bottom outlet end 2-4 is connected by the gas removal tower bottom product entrance end 1-3 of connecting pipe with turnover material heat exchanger 1, and the gas removal tower bottoms outlet end 1-4 of turnover material heat exchanger 1 is connected by connecting pipe and liquefied gas knockout tower entrance end 6-1;
Gas removal column overhead exit end 2-3 and absorbing tower bottom outlet end 23-4 converges, and gas removal column overhead exit end 2-3 and absorbing tower bottom outlet end 23-4 meet and gas removal column overhead condenser 3 inlet end through by connecting pipe, gas removal column overhead condenser 3 exit end is connected by the inlet end of connecting pipe and gas removal column overhead tank 4;
Described gas removal column overhead tank 4 is provided with liquid hydrocarbon outlet end 4-1, gaseous phase outlet end 4-2 and process water exit end 4-3; Liquid hydrocarbon outlet end 4-1 is connected by the inlet end of connecting pipe and gas removal column overhead reflux pump 5, and the exit end of gas removal column overhead reflux pump 5 is connected by connecting pipe and gas removal trim the top of column mouth 2-2; Gaseous phase outlet end 4-2 is connected by connecting pipe and absorption tower first entrance end 23-1;
Liquefied gas knockout tower tower top outlet end 6-3 is connected by the inlet end of connecting pipe and liquefied gas knockout tower overhead condenser 10, and the exit end of liquefied gas knockout tower overhead condenser 10 is connected by the inlet end of connecting pipe and liquefied gas knockout tower backflash 11, liquefied gas knockout tower backflash 11 is provided with liquefied gas knockout tower backflash first exit end 11-1 and liquefied gas knockout tower backflash second exit end 11-2, liquefied gas knockout tower backflash first exit end 11-1 is separated tower top refluxing opening 6-2 by connecting pipe with liquefied gas and connects, liquefied gas knockout tower backflash second exit end 11-2 is connected by the inlet end of connecting pipe and LPG water cooler 12, the exit end of LPG water cooler 12 is connected by the inlet end of connecting pipe and LPG surge tank 13, the exit end of LPG surge tank 13 is connected by the inlet end of connecting pipe and LPG product pump 14,
Liquefied gas knockout tower tower bottom outlet end 6-4 is connected with the inlet end of product separation tower entrance end 15-1 and lean solution feeding pump 7 respectively by connecting pipe; The exit end of lean solution feeding pump 7 is connected by the inlet end of connecting pipe and oil-poor precooler 8, the exit end of oil-poor precooler 8 is connected by the inlet end of connecting pipe and oil-poor water cooler 9, and the exit end of oil-poor water cooler 9 is connected by connecting pipe and absorption tower second entrance end 23-2;
Product separation column overhead exit end 15-3 is connected by the inlet end of connecting pipe and product separation column overhead condenser 16, the exit end of product separation column overhead condenser 16 is connected by the inlet end of connecting pipe and product separation column overhead tank 17, the exit end of product separation column overhead tank 17 is connected by the inlet end of connecting pipe and product separation column overhead reflux pump 18, and the exit end of product separation column overhead reflux pump 18 is connected with the inlet end of product separation top of tower refluxing opening 15-2 and the inlet end of light stable light hydrocarbon water cooler 19 respectively by connecting pipe;
Product separation tower tower bottom outlet end 15-4 is connected by the inlet end of connecting pipe and product separation tower column bottoms pump 20, the exit end of product separation tower column bottoms pump 20 is connected by the inlet end of connecting pipe and heavy lighter hydrocarbons water cooler 21, and the exit end of heavy lighter hydrocarbons water cooler 21 regulates the inlet end of water cooler 22 to connect by connecting pipe and heavy lighter hydrocarbons.
Exit end and the stable light hydrocarbon product discharge pipe 27 of described light stable light hydrocarbon water cooler 19 connect.
Described heavy lighter hydrocarbons regulate the exit end of water cooler 22 and heavy stable light hydrocarbon product discharge pipe 28 to connect.
Described absorption tower tower top outlet end 23-3 and fuel gas discharge nozzle 29 connect.
Exit end and the LPG product discharge pipe 26 of described LPG product pump 14 connect.
Described process water exit end 4-3 and process water discharge nozzle 25 connect.
Present embodiment principle: the thick stable light hydrocarbon come from synthesizing stable lighter hydrocarbons facilities stablizes 45 DEG C, pressure 2.5MPa, first through turnover material heat exchanger 1 heat exchange to 117.6 DEG C of gas removal tower 2, enters gas removal tower 2 and is separated, overhead product mainly comprises methane, ethane, and bottom product is with C
3above hydro carbons (comprising LPG and stable light hydrocarbon) is main.Overhead product temperature is 120 DEG C, and pressure is 2.1MPa, is mixed into two-phase mixture with absorption tower 23 bottom product.This mixture is cooled to 46 DEG C through gas removal column overhead condenser 3, delivers to gas-liquid separation in gas removal column overhead tank 4.Gas phase is sent to absorption tower 23, and process water delivers to synthesizing stable lighter hydrocarbons facilities, and liquid hydrocarbon refluxes through the pressurization of gas removal column overhead reflux pump 5 as phegma.Gas removal tower 2 bottom product temperature is 187 DEG C, and pressure is 2.14MPa, sends into liquefied gas knockout tower 6 with the thick stable light hydrocarbon of raw material after turnover material heat exchanger 1 heat exchange to 117.5 DEG C of gas removal tower 2.
Liquefied gas knockout tower 6 is mainly used to LPG to separate from thick stable light hydrocarbon.Gas removal tower 2 bottom product mainly C
3above hydro carbons, is separated further in liquefied gas knockout tower 6.Overhead product is LPG mainly, and bottom product is with C
4above hydro carbons is main.
Liquefied gas knockout tower 6 overhead product temperature is 75.5 DEG C, and pressure is 1.5MPa, is cooled to 68.5 DEG C, is got off by total condensation through the heat exchange of liquefied gas knockout tower overhead condenser 10, sends into liquefied gas knockout tower backflash 11 afterwards.C
3, C
4a liquid hydrocarbon part is back to liquefied gas knockout tower 6; Another part is cooled to 46 DEG C further through LPG water cooler 12, is forced into 1.7MPa, delivers to tank field after sending into LPG surge tank 13 as LPG product through LPG product pump 14.
Liquefied gas knockout tower 6 bottom product temperature is 197 DEG C, and pressure is 1.55MPa.Sub-fraction bottom product pressurizes through lean solution feeding pump 7, and is cooled to 40 DEG C through oil-poor precooler 8, oil-poor water cooler 9, delivers to absorption tower 23 afterwards, carries out absorption process as absorption agent to light hydrocarbon component gas; Another part is sent into product separation tower 15 and is separated further.
In product separation tower 15, be separated into light constituent hydrocarbon (overhead product) and heavy constituent hydrocarbon (bottom product) from liquefied gas knockout tower 6 bottom product.Overhead product temperature is 134 DEG C, and pressure is 0.19MPa, and be cooled to 74 DEG C through product knockout tower overhead condenser 16, total condensation is light stable light hydrocarbon, enters product separation column overhead tank 17.Light stable light hydrocarbon is forced into 0.54MPa through product knockout tower trim the top of column pump 18, and a part returns to product separation tower 15 top as phegma; Another part is cooled to 45 DEG C as product stable light hydrocarbon further through product knockout tower overhead condenser 16, delivers to intermediate tank farm.
In synthesizing stable lighter hydrocarbons, durol regulation content (being approximately 6% (wt)), is less than the requirement of 1.5% (wt) far above durol content in product stable light hydrocarbon.In order to meet the requirement of durol content in synthesizing stable lighter hydrocarbons, distilling most of durol through product separation tower 15 and being concentrated and entering in heavy stable light hydrocarbon, be i.e. bottom product.Heavy hydrocarbon temperature is 221.9 DEG C, and pressure is 0.23MPa, after being forced into 1.0MPa, regulating water cooler 22 to be cooled to 77 DEG C, send into tank field afterwards through heavy lighter hydrocarbons water cooler 21, heavy lighter hydrocarbons by product separation tower column bottoms pump 20.
In order to reduce the loss from low boiling component in synthesizing stable lighter hydrocarbons facilities water-and-oil separator gas phase and gas removal tower 2 overhead product, in absorption tower 23, utilizing partial liquefaction gas knockout tower 6 bottom product (oil-poor) to make absorption agent absorption process is carried out to these two bursts of gas phases.
Absorption tower 23 overhead product is fuel gas, and fuel gas sends into plant area's fuel gas pipe network.Bottom product is stable light hydrocarbon, wherein comprises the liquid hydrocarbon of recovery, imports in gas removal tower 2 overhead gas.
The advantage of this embodiment: this embodiment, by product separation, obtains the products such as LPG product, stable light hydrocarbon product and fuel gas respectively, can fully utilize, improve lighter hydrocarbons added value, make maximizing the benefits; Flow process and equipment is simple, turndown ratio is large, less investment, energy consumption are low, can meet various production decision, solves lighter hydrocarbons and to volatilize the safety and environmental issue brought.
Embodiment two: the difference of present embodiment and embodiment one is: described gas removal tower specification is ф 1500/3000X ~ 32310mm, and internals comprise 40 pieces of tower trays.Other is identical with embodiment one.
Embodiment three: the difference of one of present embodiment and embodiment one or two is: described liquefied gas knockout tower specification is ф 1200/ ф 2700X ~ 38493mm, and internals comprise 45 pieces of tower trays.Other is identical with embodiment one or two.
Embodiment four: the difference of one of present embodiment and embodiment one to three is: described product separation tower specification is ф 1800X ~ 31830mm, and internals comprise 38 pieces of tower trays.Other is identical with embodiment one to three.
Claims (4)
1. a method for lighter hydrocarbons tripping device lighter hydrocarbons separation, is characterized in that the method steps utilizing a kind of lighter hydrocarbons tripping device lighter hydrocarbons to be separated is as follows:
The thick stable light hydrocarbon of to be 45 DEG C and pressure by temperature be 2.5MPa passes into the thick stable light hydrocarbon entrance end of turnover material heat exchanger, thick stable light hydrocarbon heat exchange to the temperature controlling to enter turnover material heat exchanger is 117.6 DEG C, thick stable light hydrocarbon after heat exchange passes into gas removal tower, controlling gas removal tower overhead temperature is 120 DEG C, pressure is 2.1MPa, and absorbing tower bottom product is mixed with gas removal tower overhead and passes into gas removal column overhead condenser, the mixture temperature controlled after gas removal column overhead condenser condenses is 46 DEG C, condensed mixture is passed into the gas-liquid separation of gas removal column overhead tank, isolated process water is transported to synthesizing stable lighter hydrocarbons facilities by process water discharge nozzle, isolated liquid hydrocarbon is back to gas removal column overhead by gas removal column overhead reflux pump, isolated gas-phase transport is to absorption tower,
Controlling gas removal tower bottom product temperature is 187 DEG C, pressure is 2.14MPa, gas removal tower bottom product is passed into out the gas removal tower bottom product entrance end of material heat exchanger, the gas removal tower bottom product heat exchange controlling to enter turnover material heat exchanger is 117.5 DEG C to temperature, and the gas removal tower bottom product after heat exchange is passed into liquefied gas knockout tower;
Controlling liquefied gas knockout tower overhead product temperature is 75.5 DEG C, pressure is 1.5MPa, controlling liquefied gas knockout tower overhead product by heat exchange after liquefied gas knockout tower overhead condenser is 68.5 DEG C to temperature, and the liquefied gas knockout tower overhead product after heat exchange passes into liquefied gas knockout tower backflash, obtains C
3and C
4liquid hydrocarbon, by part C
3and C
4liquid hydrocarbon is back to liquefied gas separation column, by part C
3and C
4liquid hydrocarbon is cooled to 46 DEG C by LPG water cooler, then by the part C of cooling
3and C
4liquid hydrocarbon passes into LPG surge tank and LPG product pump successively, C after the pressurization of control LPG product pump
3and C
4the pressure of liquid hydrocarbon is 1.7MPa, obtains LPG product, finally LPG product is sent into tank field by LPG product discharge pipe;
Controlling liquefied gas knockout tower bottom product temperature is 197 DEG C, pressure is 1.55MPa, partial liquefaction gas knockout tower bottom product is passed into the pressurization of lean solution feeding pump, liquefied gas knockout tower bottom product after pressurization passes into oil-poor precooler and the cooling of oil-poor water cooler successively, and controlling liquefied gas knockout tower bottom product, to be cooled to temperature be 40 DEG C, finally cooled liquefied gas knockout tower bottom product passed into absorption tower;
Another part liquefied gas knockout tower bottom product is passed into product separation tower, controlling product separation tower overhead temperature is 134 DEG C, pressure is 0.19MPa, product separation tower overhead being passed into product separation column overhead condenser, to be cooled to temperature be 74 DEG C, then cooled product separation tower overhead is passed into product separation column overhead tank and product separation column overhead reflux pump successively, control product separation column overhead reflux pump and product separation tower overhead is forced into 0.54MPa, product separation tower overhead after a part being pressurizeed again passes into product separation tower, product separation tower overhead after being pressurizeed by another part passes into light stable light hydrocarbon water cooler, and to be cooled to temperature be 45 DEG C, obtain stable light hydrocarbon product, stable light hydrocarbon product is delivered to intermediate tank farm by stable light hydrocarbon product discharge pipe,
Controlling product separation tower bottom product temperature is 221.9 DEG C, pressure is 0.23MPa, product separation tower bottom product being passed into product separation tower column bottoms pump, to be forced into pressure be 1.0MPa, then the product separation tower bottom product after pressurization is passed into successively heavy lighter hydrocarbons water cooler and heavy lighter hydrocarbons to regulate water cooler to be cooled to temperature to be 77 DEG C, finally cooled product separation tower bottom product to be delivered to tank field by weight stable light hydrocarbon product discharge pipe;
Absorption tower overhead product obtains fuel gas, and fuel gas is delivered to plant area's fuel gas pipe network by fuel gas discharge nozzle.
2. the method for a kind of lighter hydrocarbons tripping device lighter hydrocarbons separation according to claim 1, is characterized in that: described gas removal tower specification is ф 1500/3000X ~ 32310mm, and internals comprise 40 pieces of tower trays.
3. the method for a kind of lighter hydrocarbons tripping device lighter hydrocarbons separation according to claim 1, is characterized in that: described liquefied gas knockout tower specification is ф 1200/ ф 2700X ~ 38493mm, and internals comprise 45 pieces of tower trays.
4. the method for a kind of lighter hydrocarbons tripping device lighter hydrocarbons separation according to claim 1, is characterized in that: described product separation tower specification is ф 1800X ~ 31830mm, and internals comprise 38 pieces of tower trays.
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| CN108017494A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of mixed light-hydrocarbon aromatic hydrocarbons |
| CN108017493A (en) * | 2016-11-04 | 2018-05-11 | 中国石油化工股份有限公司 | The method of mixed light-hydrocarbon aromatic hydrocarbons |
| CN108017494B (en) * | 2016-11-04 | 2020-10-16 | 中国石油化工股份有限公司 | Method for preparing aromatic hydrocarbon from mixed light hydrocarbon |
| CN108017493B (en) * | 2016-11-04 | 2020-10-30 | 中国石油化工股份有限公司 | Method for preparing aromatic hydrocarbon from mixed light hydrocarbon |
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