CN104817421B - A kind of method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate - Google Patents
A kind of method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate Download PDFInfo
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Abstract
A kind of method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate, relates to the method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate.The present invention solves the method that existing lighter hydrocarbons segregation apparatus lighter hydrocarbons separate, and to there is intractability big, it is impossible to efficiently separates, the problem that isolated lighter hydrocarbons can not comprehensively utilize.Thick stable light hydrocarbon is passed through turnover material heat exchanger heat exchange, controls gas removal tower overhead temperature and pressure, and overhead product condenses；Control gas removal tower tower bottom product temperature and pressure, tower tower bottom product heat exchange；Control liquefied gas knockout tower overhead product temperature and pressure, overhead product heat exchange, cool down, pressurize；Controlling liquefied gas knockout tower tower bottom product temperature and pressure, tower bottom product cools down；Control product knockout tower overhead product temperature and pressure, overhead condenser cooling, pressurization, be passed through the cooling of light stable light hydrocarbon cooler；Control product knockout tower tower bottom product temperature and pressure, pressurize, cool down.The method that the present invention separates for lighter hydrocarbons segregation apparatus lighter hydrocarbons.
Description
Technical field
The present invention relates to the method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate.
Background technology
Lighter hydrocarbons segregation apparatus is that the thick stable light hydrocarbon that synthesizing stable lighter hydrocarbons facilities comes is carried out rectification separation.By from synthesizing stable
The thick stable light hydrocarbon of lighter hydrocarbons facilities further comprises a part of dissolved hydrogen, CO2、C1～C2Light hydrocarbon gas component, and
C3～C4And C10Above heavy oil component, it is impossible to directly utilize.
Along with economic development, energy demand increases, and the comprehensive utilization of the energy becomes important development direction.Existing lighter hydrocarbons separate dress
There is the effective utilization being unfavorable for lighter hydrocarbons resource in the method putting lighter hydrocarbons separation, intractability is big, it is impossible to efficiently separate, and isolates
The problem that can not comprehensively utilize of lighter hydrocarbons.
Summary of the invention
The present invention is to solve that the method that existing lighter hydrocarbons segregation apparatus lighter hydrocarbons separate exists the effective utilization being unfavorable for lighter hydrocarbons resource,
Intractability is big, it is impossible to efficiently separate, the problem that isolated lighter hydrocarbons can not comprehensively utilize, and provides a kind of lighter hydrocarbons and separate
The method that device lighter hydrocarbons separate.
The thick stable light hydrocarbon that temperature is 45 DEG C by the present invention and pressure is 2.5MPa is passed through the thick stable of turnover material heat exchanger
Lighter hydrocarbons entrance point, the thick stable light hydrocarbon heat exchange controlling to enter turnover material heat exchanger is 117.6 DEG C to temperature, thick after heat exchange
Stable light hydrocarbon is passed through gas removal tower, and controlling gas removal tower overhead temperature is 120 DEG C, and pressure is 2.1MPa, and
Absorbing tower bottom product mixes with gas removal tower overhead and is passed through gas removal column overhead condenser, controls gas and take off
Except the condensed mixture temperature of column overhead condenser is 46 DEG C, condensed mixture is passed through gas removal column overhead tank
Gas-liquid separation, is transported to synthesizing stable lighter hydrocarbons facilities by isolated fresh water (FW) by fresh water (FW) discharge nozzle, by isolated liquid
State hydrocarbon is back to gas removal column overhead by gas removal column overhead reflux pump, and isolated gas-phase transport is to absorption tower；
Controlling gas removal tower tower bottom product temperature is 187 DEG C, and pressure is 2.14MPa, is led to by gas removal tower tower bottom product
Enter out the gas removal tower tower bottom product entrance point of material heat exchanger, control to enter the gas removal tower tower of turnover material heat exchanger
Bottom product heat exchange to temperature is 117.5 DEG C, and the gas removal tower tower bottom product after heat exchange is passed through liquefied gas knockout tower；
Controlling liquefied gas knockout tower overhead product temperature is 75.5 DEG C, and pressure is 1.5MPa, controls liquefied gas knockout tower tower top
Product is 68.5 DEG C by heat exchange after liquefied gas knockout tower overhead condenser to temperature, and the liquefied gas knockout tower tower top after heat exchange produces
Thing is passed through liquefied gas knockout tower backflash, obtains C3And C4Liquid hydrocarbon, by part C3And C4Liquid hydrocarbon is back to liquefied gas
Separation column, by part C3And C4Liquid hydrocarbon is cooled to 46 DEG C by LPG cooler, then by part C of cooling3
And C4Liquid hydrocarbon is passed through LPG surge tank and LPG product pump successively, controls C after the pressurization of LPG product pump3And C4Liquid
The pressure of hydrocarbon is 1.7MPa, obtains LPG product, finally by LPG product discharge pipe, LPG product is sent into tank field；
Controlling liquefied gas knockout tower tower bottom product temperature is 197 DEG C, and pressure is 1.55MPa, by partial liquefaction gas knockout tower tower
Bottom product is passed through the pressurization of lean solution feed pump, and the liquefied gas knockout tower tower bottom product after pressurization is passed through oil-poor precooler and lean successively
Oil cooler cools down, and control liquefied gas knockout tower tower bottom product to be cooled to temperature be 40 DEG C, finally by the liquefaction after cooling
Gas knockout tower tower bottom product is passed through absorption tower；
Another part liquefied gas knockout tower tower bottom product is passed through product knockout tower, and controlling product knockout tower overhead product temperature is
134 DEG C, pressure is 0.19MPa, product knockout tower overhead product is passed through product knockout tower overhead condenser and is cooled to temperature
It is 74 DEG C, then the product knockout tower overhead product after cooling is passed through product knockout tower overhead drum and product knockout tower successively
Overhead reflux pump, controls product knockout tower overhead reflux pump and product knockout tower overhead product is forced into 0.54MPa, then by one
Product knockout tower overhead product after part pressurization is passed through product knockout tower, the product knockout tower tower top after being pressurizeed by another part
Product is passed through light stable light hydrocarbon cooler and is cooled to temperature is 45 DEG C, obtains stable light hydrocarbon product, is led to by stable light hydrocarbon product
Cross stable light hydrocarbon product discharge pipe and be delivered to intermediate tank farm；
Controlling product knockout tower tower bottom product temperature is 221.9 DEG C, and pressure is 0.23MPa, by product knockout tower tower bottom product
Being passed through product knockout tower column bottoms pump and being forced into pressure is 1.0MPa, then by the product knockout tower tower bottom product after pressurization successively
Being passed through heavy lighter hydrocarbons cooler and heavy lighter hydrocarbons regulate cooler to be cooled to temperature be 77 DEG C, the product after finally cooling down divides
It is delivered to tank field by weight stable light hydrocarbon product discharge pipe from tower tower bottom product；
Absorption tower overhead product obtains fuel gas, and by fuel gas discharge nozzle, fuel gas is delivered to plant area's fuel gas pipe network.
Advantages of the present invention: product is separated by the present invention, respectively obtains LPG product, stable light hydrocarbon product and fuel gas etc.
Product, can comprehensively utilize, and improves lighter hydrocarbons added value, makes maximizing the benefits；Flow process and equipment is simple, operating flexibility is big,
Small investment, energy consumption are low, it is possible to meet various production decision, solve safety and environmental issue that lighter hydrocarbons volatilization brings.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of the present invention a kind of lighter hydrocarbons segregation apparatus.
Detailed description of the invention
Detailed description of the invention one: combine Fig. 1, present embodiment be a kind of lighter hydrocarbons segregation apparatus lighter hydrocarbons separate method step such as
Under:
Be 45 DEG C by temperature and pressure be 2.5MPa thick stable light hydrocarbon be passed through the thick stable light hydrocarbon of turnover material heat exchanger 1 and enter
Mouthful end 1-1, the thick stable light hydrocarbon heat exchange controlling to enter turnover material heat exchanger 1 is 117.6 DEG C to temperature, thick after heat exchange
Stable light hydrocarbon is passed through gas removal tower 2, and controlling gas removal tower 2 overhead product temperature is 120 DEG C, and pressure is 2.1MPa,
And absorption tower 23 tower bottom product mixed with gas removal tower 2 overhead product and is passed through gas removal column overhead condenser 3,
Controlling the condensed mixture temperature of gas removal column overhead condenser 3 is 46 DEG C, and condensed mixture is passed through gas
Removing tower overhead drum 4 gas-liquid separation, is transported to synthesizing stable lighter hydrocarbons by isolated fresh water (FW) by fresh water (FW) discharge nozzle 25
Device, is back to gas removal tower 2 tower top by isolated liquid hydrocarbon by gas removal column overhead reflux pump 5, isolates
Gas-phase transport to absorption tower 23；
Controlling gas removal tower 2 tower bottom product temperature is 187 DEG C, and pressure is 2.14MPa, will produce at the bottom of gas removal tower 2 tower
Thing is passed through out the gas removal tower tower bottom product entrance point 1-3 of material heat exchanger 1, controls to enter turnover material heat exchanger 1
Gas removal tower 2 tower bottom product heat exchange to temperature is 117.5 DEG C, and gas removal tower 2 tower bottom product after heat exchange is passed through liquid
Activating QI knockout tower 6；
Controlling liquefied gas knockout tower 6 overhead product temperature is 75.5 DEG C, and pressure is 1.5MPa, controls liquefied gas knockout tower 6
Overhead product is 68.5 DEG C by heat exchange after liquefied gas knockout tower overhead condenser 10 to temperature, and the liquefied gas after heat exchange separates
Tower 6 overhead product is passed through liquefied gas knockout tower backflash 11, obtains C3And C4Liquid hydrocarbon, by part C3And C4Liquid hydrocarbon
It is back to liquefied gas knockout tower 6 top, by part C3And C4Liquid hydrocarbon is cooled to 46 DEG C, so by LPG cooler 12
After will cooling part C3And C4Liquid hydrocarbon is passed through LPG surge tank 13 and LPG product pump 14 successively, controls LPG and produces
C after product pump 14 pressurization3And C4The pressure of liquid hydrocarbon is 1.7MPa, obtains LPG product, is finally passed through by LPG product
Tank field sent into by LPG product discharge pipe 26；
Controlling liquefied gas knockout tower 6 tower bottom product temperature is 197 DEG C, and pressure is 1.55MPa, by partial liquefaction gas knockout tower
6 tower bottom products are passed through lean solution feed pump 7 and pressurize, and liquefied gas knockout tower 6 tower bottom product after pressurization is passed through oil-poor pre-cooling successively
But device 8 and lean oil cooler 9 cool down, and control liquefied gas knockout tower 6 tower bottom product to be cooled to temperature be 40 DEG C, finally
Liquefied gas knockout tower 6 tower bottom product after cooling is passed through absorption tower 23；
Another part liquefied gas knockout tower 6 tower bottom product is passed through product knockout tower 15, controls product knockout tower 15 tower top and produce
Thing temperature is 134 DEG C, and pressure is 0.19MPa, and product knockout tower 15 overhead product is passed through product knockout tower overhead condensation
It is 74 DEG C that device 16 is cooled to temperature, then product knockout tower 15 overhead product after cooling is passed through product knockout tower successively
Overhead drum 17 and product knockout tower overhead reflux pump 18, control product knockout tower overhead reflux pump 18 by product knockout tower 15
Overhead product is forced into 0.54MPa, then product knockout tower 15 overhead product after part pressurization is passed through product knockout tower
15, product knockout tower 15 overhead product after being pressurizeed by another part is passed through light stable light hydrocarbon cooler 19 and is cooled to temperature and is
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 knockout tower 15 tower bottom product temperature is 221.9 DEG C, and pressure is 0.23MPa, by product knockout tower 15 tower
Bottom product is passed through product knockout tower column bottoms pump 20 and is forced into pressure is 1.0MPa, then by the product knockout tower 15 after pressurization
Tower bottom product is passed through heavy lighter hydrocarbons cooler 21 successively and heavy lighter hydrocarbons regulate cooler 22 to be cooled to temperature be 77 DEG C,
After will cooling after product knockout tower 15 tower bottom product be delivered to tank field by weight stable light hydrocarbon product discharge pipe 28；
Absorption tower 23 overhead product obtains fuel gas, and by fuel gas discharge nozzle 29, fuel gas is delivered to plant area's fuel gas pipe
Net.
A kind of lighter hydrocarbons segregation apparatus 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
Feed pump 7, oil-poor precooler 8, lean oil cooler 9, liquefied gas knockout tower overhead condenser 10, liquefied gas knockout tower
Backflash 11, LPG cooler 12, LPG surge tank 13, LPG product pump 14, product knockout tower 15, product separate
Column overhead condenser 16, product knockout tower overhead drum 17, product knockout tower overhead reflux pump 18, light stable light hydrocarbon cooler
19, product knockout tower column bottoms pump 20, heavy lighter hydrocarbons cooler 21, heavy lighter hydrocarbons regulation cooler 22 and 23 groups of absorption tower
Become；
Described turnover material heat exchanger 1 is provided with thick stable light hydrocarbon entrance point 1-1, thick stable light hydrocarbon port of export 1-2, gas
Body removing tower tower bottom product entrance point 1-3 and gas removal tower bottoms outlet end 1-4, and thick stable light hydrocarbon entrance point 1-1
Connect with thick stable light hydrocarbon port of export 1-2, gas removal tower tower bottom product entrance point 1-3 and gas removal tower tower bottom product
Port of export 1-4 connects；
Described gas removal tower 2 be provided with gas removal tower entrance point 2-1, gas removal overhead reflux mouth 2-2, gas take off
Except column overhead port of export 2-3 and gas removal tower tower bottom outlet end 2-4；
Described liquefied gas knockout tower 6 be provided with liquefied gas knockout tower entrance point 6-1, liquefied gas knockout tower fight back head piece 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 knockout tower 15 is provided with product knockout tower entrance point 15-1, product knockout tower fight back head piece 15-2, product
Knockout tower tower top outlet end 15-3 and product knockout tower tower bottom outlet end 15-4；
Described absorption tower 23 is provided with absorption tower the first entrance point 23-1, absorption tower the second entrance point 23-2, absorption tower tower top
Port of export 23-3 and absorbing tower bottom outlet end 23-4；
Thick stable light hydrocarbon entrance point 1-1 connects with thick stable light hydrocarbon feed pipe 24, and thick stable light hydrocarbon port of export 1-2 passes through
Connecting pipe connects with gas removal tower entrance point 2-1；
Gas removal tower tower bottom outlet end 2-4 is by the gas removal tower tower bottom product of connecting pipe with turnover material heat exchanger 1
Entrance point 1-3 connects, turnover material heat exchanger 1 gas removal tower bottoms outlet end 1-4 by connecting pipe with
Liquefied gas knockout tower entrance point 6-1 connects；
Gas removal column overhead port of export 2-3 converges with absorbing tower bottom outlet end 23-4, and the outlet of gas removal column overhead
End 2-3 passes through connecting pipe with absorbing tower bottom outlet end 23-4 meet and gas removal column overhead condenser 3 arrival end
Through, gas removal column overhead condenser 3 port of export is passed through mutually by the arrival end of connecting pipe with gas removal column overhead tank 4
Logical；
Described gas removal column overhead tank 4 is provided with liquid hydrocarbon outlet end 4-1, gaseous phase outlet end 4-2 and the fresh water (FW) port of export
4-3；Liquid hydrocarbon outlet end 4-1 is connected by the arrival end of connecting pipe with gas removal column overhead reflux pump 5, gas
The port of export of removing tower overhead reflux pump 5 is connected with gas removal overhead reflux mouth 2-2 by connecting pipe；Gaseous phase outlet
End 4-2 is connected with absorption tower the first entrance point 23-1 by connecting pipe；
Liquefied gas knockout tower tower top outlet end 6-3 is by the arrival end of connecting pipe with liquefied gas knockout tower overhead condenser 10
Connecting, the port of export of liquefied gas knockout tower overhead condenser 10 is by connecting pipe and liquefied gas knockout tower backflash 11
Arrival end connect；Liquefied gas knockout tower backflash 11 is provided with liquefied gas knockout tower backflash first port of export 11-1 and liquid
Activating QI knockout tower backflash second port of export 11-2, liquefied gas knockout tower backflash first port of export 11-1 pass through connecting pipe
Connecting with liquefied gas knockout tower fight back head piece 6-2, liquefied gas knockout tower backflash second port of export 11-2 passes through communicating pipe
Road connects with the arrival end of LPG cooler 12, and the port of export of LPG cooler 12 is buffered with LPG by connecting pipe
The arrival end of tank 13 connects, and the port of export of LPG surge tank 13 is by the entrance of connecting pipe with LPG product pump 14
End connects；
Liquefied gas knockout tower tower bottom outlet end 6-4 is given with product knockout tower entrance point 15-1 and lean solution respectively by connecting pipe
The arrival end of material pump 7 connects；The port of export of lean solution feed pump 7 is by the arrival end of connecting pipe with oil-poor precooler 8
Connecting, the port of export of oil-poor precooler 8 is connected by the arrival end of connecting pipe with lean oil cooler 9, oil-poor cold
But the port of export of device 9 is connected with absorption tower the second entrance point 23-2 by connecting pipe；
Product knockout tower tower top outlet end 15-3 is passed through mutually by the arrival end of connecting pipe with product knockout tower overhead condenser 16
Logical, the port of export of product knockout tower overhead condenser 16 is by the arrival end phase of connecting pipe with product knockout tower overhead drum 17
Through, the port of export of product knockout tower overhead drum 17 is by the arrival end of connecting pipe with product knockout tower overhead reflux pump 18
Connect, the port of export of product knockout tower overhead reflux pump 18 by connecting pipe respectively with product separation column refluxing opening
The arrival end of 15-2 and the arrival end of light stable light hydrocarbon cooler 19 connect；
Product knockout tower tower bottom outlet end 15-4 is connected by the arrival end of connecting pipe with product knockout tower column bottoms pump 20,
The port of export of product knockout tower column bottoms pump 20 is connected by the arrival end of connecting pipe with heavy lighter hydrocarbons cooler 21, heavy
The port of export of lighter hydrocarbons cooler 21 is connected by the arrival end of connecting pipe with heavy lighter hydrocarbons regulation cooler 22.
The port of export of described light stable light hydrocarbon cooler 19 connects with stable light hydrocarbon product discharge pipe 27.
The port of export of described heavy lighter hydrocarbons regulation cooler 22 connects with weight stable light hydrocarbon product discharge pipe 28.
Described absorption tower tower top outlet end 23-3 connects with fuel gas discharge nozzle 29.
The port of export of described LPG product pump 14 connects with LPG product discharge pipe 26.
Described fresh water (FW) port of export 4-3 connects with fresh water (FW) discharge nozzle 25.
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 of gas removal tower 2 to 117.6 DEG C, enter gas removal tower 2 and separate, tower top
Product mainly includes methane, ethane, and tower bottom product is with C3Above hydro carbons (including LPG and stable light hydrocarbon) is main.Tower
Top product temperatur is 120 DEG C, and pressure is 2.1MPa, is mixed into two-phase mixture with absorption tower 23 tower bottom product.This mixing
Thing 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
Being sent to absorption tower 23, fresh water (FW) delivers to synthesizing stable lighter hydrocarbons facilities, and liquid hydrocarbon returns through gas removal column overhead as backflow
Stream pump 5 pressurization backflow.Gas removal tower 2 tower bottom product temperature is 187 DEG C, and pressure is 2.14MPa, slightly stable with raw material
Lighter hydrocarbons send into liquefied gas knockout tower 6 after turnover material heat exchanger 1 heat exchange of gas removal tower 2 is to 117.5 DEG C.
Liquefied gas knockout tower 6 is mainly used to separate LPG from thick stable light hydrocarbon.Gas removal tower 2 tower bottom product
Mainly C3Above hydro carbons, separates in liquefied gas knockout tower 6 further.Overhead product is mainly LPG, produces at the bottom of tower
Thing is with C4Above hydro carbons is main.
Liquefied gas knockout tower 6 overhead product temperature is 75.5 DEG C, and pressure is 1.5MPa, through liquefied gas knockout tower overhead condensation
Device 10 heat exchange is cooled to 68.5 DEG C, is got off by total condensation, sends into liquefied gas knockout tower backflash 11 afterwards.C3、C4
A liquid hydrocarbon part is back to liquefied gas knockout tower 6；Another part is cooled further to 46 DEG C through LPG cooler 12, send
It is forced into 1.7MPa as LPG product through LPG product pump 14 after entering LPG surge tank 13, delivers to tank field.
Liquefied gas knockout tower 6 tower bottom product temperature is 197 DEG C, and pressure is 1.55MPa.Sub-fraction tower bottom product is through lean solution
Feed pump 7 pressurizes, and is cooled to 40 DEG C through oil-poor precooler 8, lean oil cooler 9, delivers to absorption tower 23 afterwards,
As absorbent, light hydrocarbon component gas is carried out absorption process；Another part is sent into product knockout tower 15 and is separated further.
In product knockout tower 15, it is separated into light component hydrocarbon (overhead product) from liquefied gas knockout tower 6 tower bottom product
With heavy constituent hydrocarbon (tower bottom product).Overhead product temperature is 134 DEG C, and pressure is 0.19MPa, through product knockout tower tower top
Condenser 16 is cooled to 74 DEG C, and total condensation is light stable light hydrocarbon, enters product knockout tower overhead drum 17.Light stable light hydrocarbon
Being forced into 0.54MPa through product knockout tower overhead reflux pump 18, a part returns to product knockout tower 15 top as backflow；
Another part is cooled further to 45 DEG C as product stable light hydrocarbon through product knockout tower overhead condenser 16, delivers to pans
District.
Durol regulation content (about 6% (wt)) in synthesizing stable lighter hydrocarbons, equal far above in product stable light hydrocarbon
The requirement less than 1.5% (wt) of the durene content.In order to meet the requirement of durol content, warp in synthesizing stable lighter hydrocarbons
Cross product knockout tower 15 distill major part durol be concentrated entrance weight stable light hydrocarbon in, i.e. tower bottom product.Heavy hydrocarbon temperature
Being 221.9 DEG C, pressure is 0.23MPa, product knockout tower column bottoms pump 20 after being forced into 1.0MPa, cold through heavy lighter hydrocarbons
But device 21, heavy lighter hydrocarbons regulation cooler 22 are cooled to 77 DEG C, send into tank field afterwards.
In order to reduce low boiling in synthesizing stable lighter hydrocarbons facilities oil water separator gas phase and gas removing tower 2 overhead product
The loss of component, utilize in absorption tower 23 partial liquefaction gas knockout tower 6 tower bottom product (oil-poor) make absorbent to this two
Stock gas phase carries out absorption process.
Absorption tower 23 overhead product is fuel gas, and fuel gas sends into plant area's fuel gas pipe network.Tower bottom product is stable light hydrocarbon,
Wherein comprise the liquid hydrocarbon of recovery, import in gas removal tower 2 overhead gas.
The advantage of this detailed description of the invention: product is separated by this detailed description of the invention, respectively obtains LPG product, stablizes gently
The product such as hydrocarbon product and fuel gas, can comprehensively utilize, and improves lighter hydrocarbons added value, makes maximizing the benefits；Flow process and equipment
Simply, operating flexibility is big, small investment, energy consumption are low, it is possible to meet various production decision, solves the peace that lighter hydrocarbons volatilization brings
Complete and environmental issue.
Detailed description of the invention two: the present embodiment difference from detailed description of the invention one is: described gas removal tower rule
Lattice are ф 1500/3000X～32310mm, and internals include 40 pieces of tower trays.Other is identical with detailed description of the invention one.
Detailed description of the invention three: the present embodiment difference from one of detailed description of the invention one or two is: described liquefaction
Gas knockout tower specification is ф 1200/ ф 2700X～38493mm, and internals include 45 pieces of tower trays.Other is with detailed description of the invention one
Or two is identical.
Detailed description of the invention four: the present embodiment difference from one of detailed description of the invention one to three is: described product
Knockout tower specification is ф 1800X～31830mm, and internals include 38 pieces of tower trays.Other is identical with detailed description of the invention one to three.
Claims (1)
1. a kind of method that lighter hydrocarbons segregation apparatus lighter hydrocarbons separate, it is characterised in that utilize lighter hydrocarbons segregation apparatus lighter hydrocarbons to separate
Method step is as follows:
Be 45 DEG C by temperature and pressure be 2.5MPa thick stable light hydrocarbon be passed through the thick stable light hydrocarbon import of turnover material heat exchanger
End, the thick stable light hydrocarbon heat exchange controlling to enter turnover material heat exchanger is 117.6 DEG C to temperature, and the thick stable light hydrocarbon after heat exchange leads to
Entering gas removal tower, controlling gas removal tower overhead temperature is 120 DEG C, and pressure is 2.1MPa, and by the bottom of absorbing tower
Product mixes and is passed through gas removal column overhead condenser with gas removal tower overhead, controls the condensation of gas removal column overhead
The condensed mixture temperature of device is 46 DEG C, and condensed mixture is passed through gas removal column overhead tank gas-liquid separation, will divide
The fresh water (FW) separated out is transported to synthesizing stable lighter hydrocarbons facilities by fresh water (FW) discharge nozzle, is taken off by gas by isolated liquid hydrocarbon
Except column overhead reflux pump is back to gas removal column overhead, isolated gas-phase transport is to absorption tower；
Controlling gas removal tower tower bottom product temperature is 187 DEG C, and pressure is 2.14MPa, is passed through by gas removal tower tower bottom product
Go out the gas removal tower tower bottom product entrance point of material heat exchanger, control to enter at the bottom of the gas removal tower tower passing in and out material heat exchanger
Product heat exchange to temperature is 117.5 DEG C, and the gas removal tower tower bottom product after heat exchange is passed through liquefied gas knockout tower；
Controlling liquefied gas knockout tower overhead product temperature is 75.5 DEG C, and pressure is 1.5MPa, controls liquefied gas knockout tower tower top and produces
Thing is 68.5 DEG C by heat exchange after liquefied gas knockout tower overhead condenser to temperature, the liquefied gas knockout tower overhead product after heat exchange
It is passed through liquefied gas knockout tower backflash, obtains C3And C4Liquid hydrocarbon, by part C3And C4Liquid hydrocarbon is back to liquefied gas and separates
Top of tower, by part C3And C4Liquid hydrocarbon is cooled to 46 DEG C by LPG cooler, then by part C of cooling3And C4
Liquid hydrocarbon is passed through LPG surge tank and LPG product pump successively, controls C after the pressurization of LPG product pump3And C4The pressure of liquid hydrocarbon
Power is 1.7MPa, obtains LPG product, finally by LPG product discharge pipe, LPG product is sent into tank field；
Controlling liquefied gas knockout tower tower bottom product temperature is 197 DEG C, and pressure is 1.55MPa, at the bottom of partial liquefaction gas knockout tower tower
Product is passed through the pressurization of lean solution feed pump, and the liquefied gas knockout tower tower bottom product after pressurization is passed through oil-poor precooler and oil-poor successively
Cooler cools down, and control liquefied gas knockout tower tower bottom product to be cooled to temperature be 40 DEG C, finally by the liquefaction edema caused by disorder of QI after cooling
It is passed through absorption tower from tower tower bottom product；
Another part liquefied gas knockout tower tower bottom product is passed through product knockout tower, and controlling product knockout tower overhead product temperature is
134 DEG C, pressure is 0.19MPa, product knockout tower overhead product is passed through product knockout tower overhead condenser is cooled to temperature and be
74 DEG C, then the product knockout tower overhead product after cooling is passed through product knockout tower overhead drum and product knockout tower tower top successively
Reflux pump, controls product knockout tower overhead reflux pump and product knockout tower overhead product is forced into 0.54MPa, then by a part
Product knockout tower overhead product after pressurization is passed through product knockout tower, the product knockout tower overhead product after being pressurizeed by another part
Being passed through light stable light hydrocarbon cooler and being cooled to temperature is 45 DEG C, obtains stable light hydrocarbon product, by stable light hydrocarbon product by stable
Light hydrocarbon product discharge nozzle is delivered to intermediate tank farm；
Controlling product knockout tower tower bottom product temperature is 221.9 DEG C, and pressure is 0.23MPa, is led to by product knockout tower tower bottom product
Enter product knockout tower column bottoms pump being forced into pressure is 1.0MPa, is then passed through successively by the product knockout tower tower bottom product after pressurization
It is 77 DEG C that heavy lighter hydrocarbons cooler and heavy lighter hydrocarbons regulation cooler are cooled to temperature, finally by the product knockout tower tower after cooling
Bottom product is delivered to tank field by weight stable light hydrocarbon product discharge pipe；
Absorption tower overhead product obtains fuel gas, and by fuel gas discharge nozzle, fuel gas is delivered to plant area's fuel gas pipe network.
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| 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 |
| 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 |
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| JPS6092222A (en) * | 1983-10-26 | 1985-05-23 | Mitsui Eng & Shipbuild Co Ltd | Apparatus for separating and purifying 2c fraction from hydrocarbon and method for operating the same |
| FR2796858B1 (en) * | 1999-07-28 | 2002-05-31 | Technip Cie | PROCESS AND PLANT FOR PURIFYING A GAS AND PRODUCTS THUS OBTAINED |
| FR2873710B1 (en) * | 2004-08-02 | 2006-12-01 | Inst Francais Du Petrole | PROCESS FOR TREATING A HYDROCARBONATED LOAD |
| CN102643153A (en) * | 2012-04-13 | 2012-08-22 | 中国寰球工程公司 | C<2->/C<3+> light dydrocarbon separation method integrating absorption method with fractionation method and C<2->/C<3+> light dydrocarbon separation system |
| CN103822438B (en) * | 2012-11-16 | 2016-08-03 | 中国石油天然气股份有限公司 | Shallow-cooling light hydrocarbon recovery process method |
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