CN109553504A - A kind of method and device using shallow cold oil absorption techniques recycling refinery saturation dry gas - Google Patents
A kind of method and device using shallow cold oil absorption techniques recycling refinery saturation dry gas Download PDFInfo
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- CN109553504A CN109553504A CN201710884453.9A CN201710884453A CN109553504A CN 109553504 A CN109553504 A CN 109553504A CN 201710884453 A CN201710884453 A CN 201710884453A CN 109553504 A CN109553504 A CN 109553504A
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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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
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Abstract
The present invention relates to dry gas process fields, disclose a kind of method and apparatus using shallow cold oil absorption techniques recycling refinery saturation dry gas, this method comprises: being sent into the processing of four absorption tower of carbon after saturation dry gas is successively compressed, cooled down, obtained gas phase and liquid phase is respectively fed to four desorber of naphtha scrubber and carbon；For the gas phase that recycling four desorber of carbon is handled as two concentrate gas product of carbon, obtained liquid phase is largely back to the recycling of four absorption tower of carbon, and fraction is sent to gasoline stabilizer；The liquid phase that naphtha scrubber is handled is sent into gasoline stabilizer processing, obtained liquid phase is largely back to naphtha scrubber recycling, fraction is as extraction gasoline products, the gas phase that gasoline stabilizer is handled successively carries out condensation and gas-liquid separating treatment, and obtained gas phase and liquid phase is back to suction port of compressor respectively and is sent into gasoline stabilizer, the processing of four absorption tower of carbon.Method of the invention, material consumption is low, and process is simple, invests small, C2C3 rate of recovery height.
Description
Technical field
The present invention relates to oil refinery dry gas process fields, are to be related to a kind of use shallow cold oil absorption techniques time furtherly
Receive the method and device of refinery's saturation dry gas.
Background technique
The main by-product of oil refinery dry gas from atmospheric and vacuum distillation, catalytic cracking, delayed coking, be hydrocracked, the originals such as catalytic reforming
It is interior rich in light hydrocarbons such as hydrogen, methane, ethylene, ethane, propylene, propane in the time processing and secondary processing process of oil
Resource.Oil refinery dry gas can simply be divided into two major classes: one kind is with the devices by-product such as catalytic cracking containing not compared with polyene
It is saturated dry gas, another kind of is to be free of or contain only a small amount of alkene with devices by-products such as atmospheric and vacuum distillation plus hydrogen, reformation, coking
Saturation dry gas.Oil refinery dry gas is mostly used as industry and domestic fuel, causes resource before without suitable recovery technology
Serious waste.On the other hand, ethylene is one of most important basic petrochemical raw material, production capacity and technical level by
Gradually become the important indicator for measuring a National Petrochemical industry development.It is mainly adopted in many countries, such as China, ethylene production
It is cracked with light oil, cost of material proportion in total cost of production is more than 60%.In consideration of it, recycling oil refinery dry gas
In raw material as ethylene production of carbon two, carbon third component substitution part light oil, cracking stock lighting can be made and improved
Simultaneously energy consumption can be effectively reduced in yield of ethene, to reduce the production cost of ethylene.Therefore, refinery dry gas is reasonable using gradually
Production cost of ethylene is reduced as Petrochemical Enterprises and realizes the important means of utilization of resources.
The method separated and recovered at present to oil refinery dry gas mainly has cryogenic separation method, pressure swing adsorption method, oil-absorption process
Deng various methods differ from one another.Cryogenic separation method technical maturity, the rate of recovery is high, but equipment investment is big, and energy consumption is high；Pressure-variable adsorption
For method technical maturity, it can be achieved that process control, energy consumption is lower, but product purity is low, the rate of recovery is low, and equipment is huge, takes up a large area.
Oil-absorption process mainly realizes mixed gas to the difference of each component solubility in gaseous mixture using absorbent
Separation generally absorbs the heavy constituent of C2 and C2 or more first with absorbent, isolates the incoagulable gas such as methane, hydrogen, then use
Each component in rectification method separate absorbent agent.This method has the characteristics that small scale, adaptable, investment cost is low, is current
One of most competitive oil refinery dry gas recovery technology.
CN101063048A discloses a kind of method of cold oil absorption process separating plant catalytic dry gas in use, the technique by
Compression, removing sour gas, drying and purification, absorption, desorption, cold recovery and rough segmentation and etc. composition, have absorbent at
This is cheap, loses low advantage.However, absorbing temperature in the technique is -30 DEG C to -40 DEG C, absorption temperature is low, and energy consumption is high, inhales
Receipts agent internal circulating load is big, and equipment size is big, and process CIMS is complicated, and product purity is not high.
CN101759516A discloses a kind of method of oil-absorption process separating plant catalytic dry gas, which is inhaled by compressing
Receive, desorption, reabsorb and etc. composition, using light dydrocarbon hydrocarbon be used as absorbent, recycling catalysis drying gas in two C3 fraction of carbon.So
And this method is served only for recycling catalysis drying gas, Recovery rate of ethylene is low.In addition, two concentrate pneumatic transmission of carbon is toward ethylene unit alkaline washing tower, because
And centainly need to handle and control impurity content in concentrate gas, in addition, two concentrate pneumatic transmission of carbon is toward caustic wash tower to the fortune of ethylene unit
Row is affected, and applicability is affected.
CN101759518A discloses a kind of method of shallow cold oil absorption techniques recycling plant catalytic dry gas, absorbs temperature and mentions
Up to 5~15 DEG C, therefore it is not required to propylene refrigeration machine, raw material is not required to dry and decarburization, and process is simple and two rate of recovery of carbon is high, and sets
A reabsorber has been set to recycle the absorbent for absorbing and carrying secretly in tail gas.But this method requires supplementation with more carbon four and absorbs
Agent maintains system balancing, while the operating that reabsorber needs needs to introduce a large amount of gasoline absorbent.
CN104557387A discloses a kind of system and method using shallow cold oil absorption techniques recycling refinery's mixing dry gas,
It is to be provided with kettle material of the gasoline desorber to handle reabsorber with the main distinction of CN101759518A, so that
Gasoline absorbent can be recycled, and greatly reduce the magnitude of recruitment of gasoline absorbent, but still need to supplement the more absorption of carbon four
Agent.
A kind of method that CN101812322A is also provided that shallow cold oil absorption techniques recycling plant catalytic dry gas, with
CN101759518A the difference is that, absorb tower top and finished up back and forth the absorbent carried secretly in gas using expanding machine and ice chest.
This method rate of recovery is high, is not required to introduce gasoline absorbent, but process is relative complex, and investment is relatively large, and similarly needs
Supplement more four absorbent of carbon.
In conclusion existing oil-absorption process recycling oil refinery dry gas technology is mainly used for, catalytic cracked dry gas etc. is unsaturated to be done
The recycling of ethylene in gas, and the problems such as generally existing absorbent consumption is big, material consumption is high, technique applicability is limited.
Summary of the invention
For realize to refinery be saturated dry gas efficiently and reliably recycled, while solve absorbent consumption greatly, material consumption
The problems such as high, the present invention provides a kind of method and devices using shallow cold oil absorption techniques recycling refinery saturation dry gas.This hair
Bright method uses shallow cold oil absorption techniques, by absorbing-desorbing twice, recycles two component of carbon from refinery's saturation dry gas, obtains
The two concentrate pneumatic transmission of carbon arrived does not need removing sour gas device, device for deoxidizing and drying device etc. toward Furnace of Ethylene Cracking Plant,
The rate of recovery is high, and absorbent consumption is few, energy consumption is lower, and with low investment and process is simple.
The present invention provides a kind of method using shallow cold oil absorption techniques recycling refinery saturation dry gas, and this method includes following
Step:
(1) it is sent into the processing of four absorption tower of carbon after refinery's saturation dry gas successively being compressed, cooled down, at four absorption tower of carbon
It manages obtained gas phase and liquid phase is respectively fed to naphtha scrubber and the processing of four desorber of carbon；
(2) gas phase for handling naphtha scrubber is discharged into fuel gas pipe network, liquid phase is sent into gasoline stabilizer processing；
(3) as two concentrate gas product of carbon, four desorber of carbon handles to obtain the gas phase that recycling four desorber of carbon is handled
Liquid phase be largely back to four absorption tower of carbon recycling, fraction send to gasoline stabilizer processing；
(4) liquid phase that gasoline stabilizer is handled largely is back to naphtha scrubber to be recycled, fraction is made
It is sent out outside battery limit (BL) for extraction gasoline products, the gas phase that gasoline stabilizer is handled successively carries out condensation process and gas-liquid separation
Processing, the gas phase and liquid phase that gas-liquid separation is handled are back to suction port of compressor respectively and are sent into gasoline stabilizer, carbon four is inhaled
Receive tower processing.
In method of the invention, refinery is saturated dry gas can be for from the devices such as atmospheric and vacuum distillation plus hydrogen, reformation, coking
The saturation dry gas of by-product, generally, wherein contain 20-40mol% methane, 10-25mol% ethane, 5-20mol% propane,
Remaining group is divided into hydrogen, carbon four and the above component, saturated water etc..
In order to facilitate subsequent processing, under preferable case, the processing method of the compression includes: by the pressure of refinery's saturation dry gas
Power is improved to 3-5MPaG；It is further preferred that the boil down to multi-stage compression, the present invention do not have the number of segment of compression processing
Special regulation, such as can be two sections of compressions or three sections of compressions.
In the case of process of the present invention it is preferred, the processing method of the cooling includes: the material cooling for obtaining compression
To 5-20 DEG C, preferably to 10-15 DEG C, it is further preferred that the refrigerant that cooling treatment uses is water at low temperature or liquefied ammonia, then into one
Preferably, water at low temperature is prepared step by lithium-bromide absorption-type refrigerating machine, and temperature can be 5 DEG C or 7 DEG C.
In the case of process of the present invention it is preferred, the method for four absorption tower of the carbon processing includes: will be after compression, cooling
Refinery's saturation dry gas supply to contacting it with four absorbent of carbon in four absorption tower of carbon, the number of theoretical plate on four absorption tower of carbon is
35-45, operating pressure 3-4.5MPaG, tower top temperature are 5-25 DEG C, and bottom temperature is 100-160 DEG C, preferably 110-130
℃。
It will be understood by those skilled in the art that supplying to carbon four and absorbing compression, saturation oil refinery dry gas after cooling
The embodiment for contacting it with four absorbent of carbon can be with are as follows: four absorbent of carbon sprayed at the top of four absorption tower of carbon, with
The dry gas material counter current contacting entered in the middle part of from four absorption tower of carbon, four absorbent of carbon absorb C2 and more heavy constituent in material, so
The gaseous phase materials of four absorption tower tower top of carbon (predominantly unabsorbed methane, hydrogen body) is supplied to naphtha scrubber afterwards and is recycled
Four absorbent of carbon and a small amount of unabsorbed carbon two, three component of carbon wherein carried secretly, by the liquid phase material of four absorption tower tower reactor of carbon
(i.e. four absorbent of rich carbon) supply to four desorber of carbon carries out four desorption of carbon processing.
In the case of process of the present invention it is preferred, the method for four desorber of the carbon processing includes: will be at four absorption tower of carbon
It manages obtained liquid phase material to supply to being separated in four desorber of carbon, the number of theoretical plate of four desorber of carbon is 35-45, operation pressure
Power is 2.5-3.5MPaG, and tower top temperature is 55-65 DEG C, and bottom temperature is 100-160 DEG C, preferably 110-130 DEG C.
It is solved it will be understood by those skilled in the art that supplying the liquid phase material that four absorption tower of carbon is handled to carbon four
Inhaling in tower the embodiment that is separated can be with are as follows: supplies the liquid phase material from four absorption tower tower reactor of carbon to four desorber of carbon
Middle part, desorbing the gaseous phase materials that column overhead obtains in carbon four is two concentrate gas of carbon (rich in ethane and propane)；In four desorber of carbon
The liquid phase material that tower reactor obtains is poor four absorbent of carbon, and the most of of poor four absorbent of carbon returns after stage-by-stage heat exchange, cooling
It is back to four absorption tower of carbon to be recycled, under preferable case, poor four absorbent of carbon is cooled to 5-20 DEG C, further preferably to 10-
Four absorption tower absorption of carbon processing is back to after 15 DEG C, remaining fraction is supplied to gasoline stabilizer.For carbon four in guarantee system
The carbon four on absorption tower absorbs agent flux, it is further preferred that supplementing into four absorption tower of carbon new when carrying out the absorption processing of carbon four
Fresh four absorbent of carbon.The present invention does not specially require the temperature of four absorbent of fresh carbon of supplement itself, as long as supplying to carbon
Temperature when four absorption towers is 5-20 DEG C, preferably 10-15 DEG C.
The ethane of 30-80mol% and the propane of 10-50mol%, oxygen, methane content are mainly contained in two concentrate gas of carbon
It is low and controllable, it can be directly as the raw material of cracking of ethylene.
It will be understood by those skilled in the art that in the present invention, in four desorber tower reactor extraction section liquid phase material of carbon,
And the purpose for supplementing fresh four absorbent of carbon is to prevent the accumulation of heavy constituent in four absorbent of cyclic carbon, so as to cause the absorption of carbon four
Tower and four desorber bottom temperature of carbon are excessively high.Composition according to dry gas raw material is different, the liquid phase material that four desorption of carbon is handled
Four absorbent of extracted amount and fresh carbon magnitude of recruitment it is also different, for example the C4+ component in dry gas raw material is fewer, can be in carbon
Four desorber tower reactor liquid phase materials are taken out less or only interval extracts C 4 materials out；If C4+ is relatively more in dry gas, need to extract out
The amount of C 4 materials is then bigger.
It will be understood by those skilled in the art that in the present invention, in four desorber tower reactor extraction section liquid phase material of carbon
The purpose handled to gasoline stabilizer is supplied, is that the Partial Liquid Phase material is separated into four component of carbon and carbon in gasoline stabilizer
Four or more components, wherein four groups of dispensings of carbon to four absorption tower of carbon are used as absorbent, and four or more carbon group dispensing to gasoline absorbs
Tower is used as gasoline absorbent, to reduce the magnitude of recruitment of fresh absorbent.
Comprehensively consider the above, according to the present invention a kind of specific embodiment, is back to the recycling of four absorption tower of carbon
The liquid phase that handles of four desorber of the carbon account for 90% or more of the liquid phase that four desorber of carbon is handled.
In method of the invention, four absorbent of carbon is to be carried out when carbon four absorbs processing in four absorption tower of carbon for absorbing pressure
The absorbent of C2 component and more heavy constituent in contracting dry gas material can be the various suctions for meeting above-mentioned requirements commonly used in the art
Agent is received, C-4-fraction is not limited only to.Specifically, there is no particular limitation for four absorbent of carbon by the present invention, Ke Yiwei
Various C3 fractions, C-4-fraction or C5 fraction commonly used in the art, under preferable case, four absorbent of carbon is containing just
The C-4-fraction of butane and iso-butane, containing saturation C3 fraction and C-4-fraction saturation liquefied gas or contain pentane
With the C5 fraction of isopentane, C-4-fraction further preferably containing normal butane and iso-butane or evaporated containing saturated carbon three
Divide the saturation liquefied gas with C-4-fraction.In order to make full use of resource and reduce cost, four absorbent of carbon preferably comes from refinery
Four absorbent of carbon, liquefied gas further preferably from refinery, mixing C-4-fraction.The present invention is for four absorbent of carbon
There is no particular limitation for dosage, those skilled in the art can determines according to actual conditions, this by those skilled in the art public affairs
Know, details are not described herein.
In the case of process of the present invention it is preferred, the processing method of the naphtha scrubber includes: will be at four absorption tower of carbon
It manages obtained gaseous phase materials to supply to contacting it with gasoline absorbent in naphtha scrubber, the number of theoretical plate of naphtha scrubber is
15-25, operating pressure 2.5-4MPaG, tower top temperature are 20-30 DEG C, and bottom temperature is 25-40 DEG C.
It will be understood by those skilled in the art that supplying the gaseous phase materials that four absorption tower absorption of carbon is handled to vapour
The embodiment for contacting it with gasoline absorbent can be with are as follows: by the gaseous phase materials from four absorption tower tower top of carbon
Gasoline absorbent is entered from tower top to naphtha scrubber bottom, makes gas by (predominantly unabsorbed methane, hydrogen body) supply
Phase materials are contacted with gasoline absorbent, and gasoline absorbent absorbs four absorbent of carbon carried secretly in gaseous phase materials, is not absorbed on a small quantity
Carbon two, three component of carbon, naphtha scrubber tower top and tower reactor respectively obtain gaseous phase materials and liquid phase material (i.e. rich gasoline absorb
Agent), supply the fuel gas pipe network to outside battery limit (BL) for gaseous phase materials as fuel gas, by liquid phase material supply to gasoline stabilizer into
Row gasoline stablizes processing.
It will be understood by those skilled in the art that the gasoline absorbent in the present invention is in naphtha scrubber for inhaling
Receive four absorbent of carbon carried secretly in the gaseous phase materials from four absorption tower tower top of carbon, a small amount of unabsorbed carbon two, three component of carbon
Absorbent, can be the various absorbents for meeting above-mentioned requirements commonly used in the art.Preferably, the gasoline absorbent is vapour
One of oil, heavy naphtha and Aromatic raffinate are a variety of, further preferably gasoline, much further preferably from from refinery
Stable gasoline.There is no particular limitation for the dosage of gasoline absorbent by the present invention, and those skilled in the art can be according to reality
Border situation determines that this is known to those skilled in the art, and details are not described herein.
In the case of process of the present invention it is preferred, the method for the gasoline stabilizer processing includes: will be at four desorber of carbon
It manages the liquid phase material that obtained fraction liquid phase material and naphtha scrubber are handled to supply to gasoline stabilizer, gasoline is steady
The number of theoretical plate for determining tower is 25-35, and operating pressure 0.5-1MPaG, tower top temperature is 40-80 DEG C, bottom temperature 120-150
℃。
It will be understood by those skilled in the art that fraction liquid phase material and gasoline that four desorber tower reactor of carbon is extracted out
The liquid phase material that absorbent absorption is handled supplies the embodiment to gasoline stabilizer can be with are as follows: will desorb from carbon four
The liquid phase material of tower reactor is supplied to the top of gasoline stabilizer, and the liquid phase material from naphtha scrubber tower reactor is supplied to gasoline
The middle part of stabilizer carries out gasoline and stablizes processing, and the gaseous phase materials that gasoline stabilizer tower top is obtained carry out condensation process；By vapour
The liquid phase material (poor gasoline absorbent) that oily stabilizer tower reactor obtains extraction fraction after stage-by-stage heat exchange, cooling is used as extraction vapour
Oil product sends out battery limit (BL), remaining liquid phase material is back to naphtha scrubber absorption processing, while for gasoline in guarantee system
The gasoline on absorption tower absorbs agent flux, it is further preferred that supplementing into naphtha scrubber new when carrying out gasoline absorption processing
Fresh gasoline absorbent.The present invention does not specially require the temperature of the fresh gasoline absorbent of supplement itself, as long as supplying to vapour
Temperature when oil-absorption tower is 5-20 DEG C, preferably 10-15 DEG C.
It will be understood by those skilled in the art that in the present invention, in gasoline stabilizer tower reactor extraction section liquid phase material,
And the purpose for supplementing fresh gasoline absorbent is to prevent the accumulation of heavy constituent in recycle gasoline absorbent, is stablized so as to cause gasoline
Tower bottom temperature is excessively high, and the height of the visual bottom temperature of extracted amount is adjusted.A kind of specific embodiment according to the present invention,
It is back to the liquid phase that the gasoline stabilizer that naphtha scrubber is recycled is handled and accounts for what gasoline stabilizer was handled
95% or more of liquid phase.
In the case of process of the present invention it is preferred, the method for the condensation process includes: to handle to obtain by gasoline stabilizer
Gaseous phase materials be cooled to 5-20 DEG C, preferably to 10-15 DEG C；It is further preferred that the condensation process is cold in gasoline stabilizer
It is carried out in condenser；
In the case of process of the present invention it is preferred, the method for the gas-liquid separation processing includes: to obtain condensation process
Material supplies to gasoline stabilizer return tank and carries out gas-liquid separation, and the operating pressure of the gasoline stabilizer return tank is 0.5-
1MPaG, temperature are 5-20 DEG C.
In method of the invention, for the liquid phase material that stabilizer return tank is handled, it is back to the suction of four absorption tower of carbon
The weight ratio of the material and the material for being back to gasoline stabilizer processing of processing is received, those skilled in the art can be according to the actual situation
It is adjusted, is back to the amount of the material of gasoline stabilizer processing for adjusting gasoline stabilizer tower top and tower reactor composition, and it is dry
Gas composition is related.A kind of specific embodiment according to the present invention, the liquid phase that gas-liquid separation is handled are sent into gasoline stabilizer, carbon
The weight ratio on four absorption towers is 1:2-5.
It will be understood by those skilled in the art that carbon four to be desorbed to the liquid phase object of tower reactor extraction in method of the invention
Material supply is separated to gasoline stabilizer, and after condensation process and gas-liquid separating treatment, four component of carbon therein is as carbon
Four absorbents, which are back to four absorption tower of carbon, can reduce the magnitude of recruitment of fresh carbon four, and carbon four and the above component are as gasoline absorbent
The magnitude of recruitment of fresh gasoline can be reduced by being back to naphtha scrubber then.
Process of the present invention it is preferred ground, according to four absorption tower of carbon, naphtha scrubber, four desorber of carbon, gasoline stabilizer
Sequence, operating pressure successively declines, and each tower material can enter upstream device by pressure difference.
The present invention also provides a kind of device of recycling refinery saturation dry gas, which includes: residue gas compressor, dry gas cooling
Device, four absorption tower of carbon, four desorber of carbon, naphtha scrubber, gasoline stabilizer, gasoline stabilizer condenser and gasoline stabilizer return
Flow tank；
The residue gas compressor, dry gas cooler and four absorption tower of carbon are sequentially communicated according to logistics direction；
The four absorption tower tower top of carbon is connected to naphtha scrubber, and tower reactor is connected to four desorber of carbon；
The naphtha scrubber tower top is connected with fuel gas extraction pipeline, and tower reactor is connected to gasoline stabilizer；
The carbon four desorbs column overhead and is connected with two concentrate gas product of carbon extraction pipeline, and tower reactor pipeline is divided into two, one
It is connect with four absorption tower of carbon, another connect with gasoline stabilizer；
The gasoline stabilizer tower top is sequentially communicated gasoline stabilizer condenser and gasoline stabilizer return tank, tower reactor pipeline
It is divided into two, one connect with naphtha scrubber, and another produces pipeline for extraction gasoline products；
The gasoline stabilizer return tank tower top is connected to residue gas compressor, and tower reactor pipeline is divided into two, a connection vapour
Oily stabilizer, another four absorption tower of connection carbon.
Preferably, four absorption tower of carbon is connected with fresh four absorbent of carbon and makes up line, the naphtha scrubber connection
There is fresh gasoline absorbent to make up line.
In the device of the invention, the mode for being interconnected and connecting between each equipment and between pipeline and equipment can basis
It needs to be arranged.For example, to obtain better assimilation effect, fresh four absorbent of carbon makes up line and four desorber tower reactor of carbon
One of pipeline is connected to the top on four absorption tower of carbon, and analogously, the fresh gasoline absorbent makes up line and gasoline
One of stabilizer tower reactor pipeline is connected to the top of naphtha scrubber.In the dry gas cooler connection four absorption tower of carbon
Portion, the middle part of four absorption tower of carbon connection, four desorber of carbon, the lower part of four absorption tower of the carbon connection naphtha scrubber are described
Naphtha scrubber is connected to the middle part of gasoline stabilizer, the top of four desorber of the carbon connection gasoline stabilizer.Art technology
Personnel should be understood that each equipment of apparatus of the present invention is not limited to the connection type of foregoing description.
In the device of the invention, it is preferable that four absorption tower tower reactor of carbon and four desorber tower reactor of carbon are provided with reboiler, with
Guarantee that the light components content such as oxygen, methane and two rate of recovery of carbon reach sets requirement in two concentrate gas of carbon.Gasoline stabilizer setting
There is reboiler, to achieve the purpose that the extraction liquid phase for making gasoline absorbent regeneration and separation from the desorption tower reactor of carbon four.Each tower is again
The heat medium for boiling device can use low-pressure steam, can also use refinery's low temperature hot oil or low-temperature water heating, especially carbon four
The reboiler of four desorber of absorption tower and carbon, since temperature is lower, preferably low temperature hot oil is heated, and refinery can be made full use of rich
Heat can also reduce process energy consumption.
The method and apparatus of recycling refinery saturation dry gas of the invention, have the advantage that
(1) method of the invention, using shallow cold oil absorption techniques, by absorbing-desorbing twice, from refinery's saturation dry gas
High efficiente callback ethane and propane, obtained two concentrate pneumatic transmission of carbon toward Furnace of Ethylene Cracking Plant, do not need removing sour gas device,
Device for deoxidizing and drying device etc., two carbon of carbon, three component recovery is high, low energy consumption, with low investment and process is simple.
(2) in method of the invention, the liquid phase extraction fraction that four desorber of carbon is handled is sent to gasoline stabilizer
Processing, the advantage is that: in a first aspect, because containing a small amount of carbon four and the above heavy constituent in oil refinery dry gas, these components all enter
In the liquid phase handled to four desorber of carbon, therefore, fraction is extracted out from the liquid phase and is sent to gasoline stabilizer, can avoid weight
Component accumulates in four absorptions of carbon-desorption system and causes the bottom temperature of four desorber of four absorption tower of carbon and carbon excessively high, eliminates
The risk of tower reactor coking；Second aspect, the liquid phase extraction fraction handled from four desorber of carbon are sent to from gasoline stabilizer
Reason, the carbon four in it is separated with four or more component of carbon, four component of carbon is incorporated into four absorbent of cyclic carbon, can be reduced
The magnitude of recruitment of fresh carbon four, four or more component of carbon are incorporated into recycle gasoline absorbent, can equally reduce gasoline absorbent
Magnitude of recruitment, therefore, absorbent consumption needed for system are greatly lowered.
(3) in method of the invention, for recycling four absorbent of carbon of C2C3 component in refinery's saturation dry gas and being used for
The gasoline suction of four absorbent of carbon, a small amount of unabsorbed carbon two, three component of carbon carried secretly in recycling four absorption tower tower top tail gas of carbon
Agent is received, is easy to get, it is low in cost.
(4) in the techniques such as traditional cryogenic separation and the absorption of deep cooling oil, because of low operation temperature, equipment needs to use cryogenic carbon
Steel, and in method of the invention, the minimum operating temperature of process system is not less than 0 DEG C, and ordinary carbon steel can be used in equipment and pipeline,
Save great amount of investment.
Other features and advantages of the present invention will then part of the detailed description can be specified.
Detailed description of the invention
Exemplary embodiment of the invention is described in more detail in conjunction with the accompanying drawings.
Fig. 1 is the structural schematic diagram of the device of recycling refinery saturation dry gas of the invention.
Description of symbols
1 residue gas compressor；2 dry gas coolers；3 carbon, four absorption tower；4 carbon, four desorber；5 naphtha scrubbers；6 gasoline are stablized
Tower；7 gasoline stabilizer condensers；8 gasoline stabilizer return tanks；9 refineries are saturated dry gas；10 supplement carbon four；11 carbon, two concentrate gas
Product；12 fuel gas；13 supplement gasoline；14 extraction gasoline products.
Specific embodiment
The present invention will be described in detail by the following examples, but is not intended to limit the present invention.
In following embodiment and comparative example, the composition of refinery's saturation dry gas from coking plant is as shown in table 1.
Table 1
Embodiment 1
The method and apparatus that the present embodiment is used to illustrate recycling refinery saturation dry gas of the invention.
The device includes: residue gas compressor 1, dry gas cooler 2, four absorption tower 3 of carbon, four desorber 4 of carbon, naphtha scrubber
5, gasoline stabilizer 6, gasoline stabilizer condenser 7 and gasoline stabilizer return tank 8；
The residue gas compressor 1, dry gas cooler 2 and four absorption tower 3 of carbon are sequentially communicated according to logistics direction；Residue gas compressor
1 is connected with refinery's saturation dry gas pipeline；
Four absorption tower of carbon, 3 tower top is connected to the lower part of naphtha scrubber 5, and tower reactor and the middle part of four desorber 4 of carbon connect
It is logical；
5 tower top of naphtha scrubber is connected with fuel gas extraction pipeline, and tower reactor is connected to the middle part of gasoline stabilizer 6；
Four desorber of carbon, 4 tower top is connected with two concentrate gas product of carbon extraction pipeline, and tower reactor pipeline is divided into two, one
It is connect with the top on four absorption tower 3 of carbon, another connect with the top of gasoline stabilizer 6；
6 tower top of gasoline stabilizer is sequentially communicated gasoline stabilizer condenser 7 and gasoline stabilizer return tank 8, tower reactor
Pipeline is divided into two, and one connect with 5 top of naphtha scrubber, and another produces pipeline for extraction gasoline products；
Connect after 8 overhead line of gasoline stabilizer return tank and refinery's saturation dry gas pipeline converge with residue gas compressor 1
Logical, tower reactor pipeline is divided into two, 6 top of connection gasoline stabilizer, another with one of four desorber of carbon, 4 tower reactor pipeline
The top on four absorption tower 3 of carbon is connected after converging；
Four absorption tower 3 of carbon is connected with fresh four absorbent of carbon and makes up line, and the naphtha scrubber 5 is connected with fresh
Gasoline absorbent makes up line.
This method comprises: supplying the saturation dry gas 9 that pressure is 0.5MPaG to residue gas compressor 1, at three sections of compressions
Reason improves dry gas pressure to 4MPaG.Then by pressurized dry gas through the lithium-bromide absorption-type refrigerating machine system of dry gas cooler 2
Supply is to four absorption tower of carbon, 3 middle part after 7 DEG C of standby cold water are cooled to 15 DEG C, in four absorption tower 3 of carbon, using the liquid from refinery
Change gas as four absorbent (flow 85t/h) of carbon, sprayed into from the tower top on four absorption tower 3 of carbon, with compression dry gas counter current contacting.Its
In, the number of theoretical plate on four absorption tower 3 of carbon is 41, and operating pressure 3.8MPaG, tower top temperature is 18.9 DEG C, and bottom temperature is
121.6℃.Four absorption tower 3 of carbon is using the 0.5MPaG low-pressure steam heating from refinery.It will be from four absorption tower of carbon, 3 tower reactor
Liquid phase material is supplied to the processing of four desorber 4 of carbon, and by the gaseous phase materials from four absorption tower of carbon, 3 tower top, (gaseous phase materials are mainly
Unabsorbed methane, hydrogen body) it supplies to naphtha scrubber 5.
Liquid phase material from four absorption tower of carbon, 3 tower reactor is supplied by pressure difference to four desorber of carbon, 4 middle part.Four desorber of carbon
4 number of theoretical plate is 40, operating pressure 2.8MPaG, and tower top temperature is 61.6 DEG C, and bottom temperature is 128.8 DEG C.Carbon four desorbs
Tower 4 obtains two concentrate gas product 11 of carbon using the 0.5MPaG low-pressure steam heating from refinery, four desorber of carbon, 4 tower top, directly
It is sent into the ethane furnace of ethylene unit.The liquid phase material for extracting 7.6wt% out from the liquid phase material from four desorber of carbon, 4 tower reactor supplies
To 6 top of gasoline stabilizer, and remaining liquid phase material is cooled to after 15 DEG C and is back to four absorption tower 3 of carbon and is recycled, together
When introduce a small amount of fresh liquefied gas from refinery as supplement carbon 4 10 supply to four absorption tower 3 of carbon.
Gaseous phase materials from four absorption tower of carbon, 3 tower top are supplied by pressure difference to 5 bottom of naphtha scrubber, are sprayed with from tower top
Gasoline absorbent (flow 20t/h) contact entered, the gasoline absorbent are the stable gasoline from refinery.Wherein, gasoline absorbs
The number of theoretical plate of tower is 20, operating pressure 3.5MPaG, and tower top temperature is 22.4 DEG C, and bottom temperature is 33.3 DEG C.Vapour will be come from
The liquid phase material of 5 tower reactor of oil-absorption tower is supplied to 6 middle part of gasoline stabilizer, by the gaseous phase materials from 5 tower top of naphtha scrubber
I.e. fuel gas 12 (being predominantly substantially free of the methane, hydrogen body of carbon two and the above component) is supplied to fuel gas pipe network.
Extraction carbon four from four desorber of carbon, 4 tower reactor enters 6 top of gasoline stabilizer, comes from 5 tower reactor of naphtha scrubber
Liquid phase material enter the middle part of gasoline stabilizer 6 by pressure difference, wherein the number of theoretical plate of gasoline stabilizer 6 is 30, and operating pressure is
0.8MPaG, tower top temperature are 52.7 DEG C, and bottom temperature is 140.0 DEG C.Gasoline stabilizer 6 uses refinery 0.5MPaG low-pressure steam
Heating, the liquid phase material of the liquid phase material extraction 2.7wt% that 6 tower reactor of gasoline stabilizer is obtained as extracting gasoline products 14 out,
Rest part is back to naphtha scrubber 5, while introducing a small amount of fresh stable gasoline from refinery as supplement gasoline 13
It supplies to naphtha scrubber 5.The gaseous phase materials that 6 tower top of gasoline stabilizer obtains are supplied to general in gasoline stabilizer condenser 7
Supply to gasoline stabilizer return tank 8 carries out gas-liquid separation, the operating pressure of gasoline stabilizer return tank 8 after it is cooled to 15 DEG C
For 0.75MPaG, the gaseous phase materials (predominantly C4 and following fraction) that 8 tank deck of gasoline stabilizer return tank obtains are back to dry
The liquid phase material (predominantly C 4 fraction) that 8 tank bottom of gasoline stabilizer return tank obtains is back to gasoline stabilizer by air compressor 1
3 tower top of 6 tower tops and four absorption tower of carbon, wherein be back to the material of four absorption tower of carbon, 3 tower top and be back to 6 tower of gasoline stabilizer
The weight ratio of the material on top is 3.5:1.
In the method for the present embodiment, it is 98.1% that two concentrate gas of carbon, the composition for extracting gasoline material out, which are shown in Table 2, the C2 rate of recovery,
C2C3 overall recovery is 96.2%.
Table 2
Comparative example 1
Using in CN104557387A similar process, (because table 1 is is saturated dry gas, no setting is required to recycle dry gas in table 1
Crude tower).The difference of process and process in embodiment 1 that the comparative example process uses is, for anti-four absorptions of blocking-desorption system
The accumulation of heavy constituent in system, liquid phase extraction a part that four desorber of carbon, 4 tower reactor is handled are straight as extraction four product of carbon
Battery limit (BL) is picked out, and is no longer sent to the processing of gasoline stabilizer 6.
In the method for this comparative example, the composition of two concentrate gas of carbon, extraction carbon four and extraction gasoline is shown in Table 3, the C2 rate of recovery and is
98.0%, C2C3 overall recovery are 92.7%.
Table 3
By four absorption tower of carbon in embodiment 1 and comparative example 1, the operating condition, fresh of four desorber of carbon and gasoline stabilizer
Magnitude of recruitment and the C2 rate of recovery, the C2C3 overall recovery of absorbent are summarized, and the results are shown in Table 4.
Table 4
As shown in Table 4, embodiment 1 is compared with comparative example 1, the operating condition substantially phase of four desorber of four absorption tower of carbon and carbon
When only four desorption tower reboiler load of carbon is more slightly higher in comparative example 1.For gasoline stabilizer, because in embodiment 1 by carbon four
Liquid phase material extraction a part (i.e. extraction carbon four) of desorption tower reactor is sent to gasoline stabilizer processing, and the hot and cold negative of the tower is caused
Lotus is all larger than comparative example 1.But just because of one more extraction carbon four of gasoline stabilizer are fed in embodiment 1, the tower is reduced
The average molecular weight of interior material, thus the bottom temperature of the tower is only 140 DEG C, it can be using 0.5MPaG low-pressure steam as heat
Source, and the bottom temperature of gasoline stabilizer is 163 DEG C in comparative example 1, can only use the steam of higher temperatures position, that is, is not less than
The steam of 1.0MPaG is as heat source.In general, within embodiment 1 is than 1 energy consumption of comparative example only high 4%.
But in order to control on four absorption tower of carbon and four desorber bottom temperature of carbon within 130 DEG C to avoid tower reactor knot
Coke, embodiment 1 only needs four absorbent of fresh carbon of supplement 350KG/h, and comparative example 1 requires supplementation with 6000KG/h, is much larger than
Embodiment 1.Similarly, to avoid gasoline absorption-systems stabilisation heavy constituent accumulation, the fresh gasoline that embodiment 1 need to supplement absorbs
Dosage is also far below comparative example 1.In addition, the C2C3 overall recovery of embodiment 1 is also high in the case where the C2 rate of recovery is essentially identical
In comparative example 1.
By comparing it is found that in the case where energy consumption is increased slightly, the magnitude of recruitment of absorbent can be greatly reduced in embodiment 1
And the rate of recovery of C2C3 can be improved.Therefore, method of the invention has low material consumption, C2C3 rate of recovery height, process simply and energy consumption
More low significant advantage.
Various embodiments of the present invention are described above, above description is exemplary, and non-exclusive, and
It is not limited to disclosed each embodiment.Without departing from the scope and spirit of illustrated each embodiment, for this skill
Many modifications and changes are obvious for the those of ordinary skill in art field.
Claims (12)
1. a kind of method using shallow cold oil absorption techniques recycling refinery saturation dry gas, which is characterized in that this method comprises:
(1) it is sent into the processing of four absorption tower of carbon after refinery's saturation dry gas successively being compressed, cooled down, four absorption tower of carbon is handled
To gas phase and liquid phase be respectively fed to naphtha scrubber and four desorber of carbon processing；
(2) gas phase for handling naphtha scrubber is discharged into fuel gas pipe network, liquid phase is sent into gasoline stabilizer processing；
(3) gas phase that recycling four desorber of carbon is handled is as two concentrate gas product of carbon, the liquid that four desorber of carbon is handled
It is mutually largely back to the recycling of four absorption tower of carbon, fraction is sent to gasoline stabilizer processing；
(4) liquid phase that gasoline stabilizer is handled largely is back to naphtha scrubber to be recycled, fraction is as pumping
Gasoline products are sent out outside battery limit (BL) out, and the gas phase that gasoline stabilizer is handled successively carries out at condensation process and gas-liquid separation
Reason, the gas phase and liquid phase that gas-liquid separation is handled are back to suction port of compressor respectively and are sent into gasoline stabilizer, carbon four absorbs
Tower processing.
2. according to the method described in claim 1, wherein, the processing method of the compression includes: by the pressure of refinery's saturation dry gas
Power is improved to 3-5MPaG；Preferably, the boil down to multi-stage compression, further preferably two sections compressions or three sections of compressions.
3. according to the method described in claim 1, wherein, the processing method of the cooling includes: that the material that obtains compression is cold
But to 5-20 DEG C, preferably to 10-15 DEG C, it is further preferred that the refrigerant that cooling treatment uses is water at low temperature or liquefied ammonia.
4. according to the method described in claim 1, wherein, the method for four absorption tower of the carbon processing includes: will be after compression, cooling
Refinery's saturation dry gas supply to contacting it with four absorbent of carbon in four absorption tower of carbon, the number of theoretical plate on four absorption tower of carbon is
35-45, operating pressure 3-4.5MPaG, tower top temperature are 5-25 DEG C, and bottom temperature is 100-160 DEG C；
Preferably, when carrying out the absorption processing of carbon four, fresh four absorbent of carbon is supplemented into four absorption tower of carbon.
5. according to the method described in claim 4, wherein, four absorbent of carbon be the C-4-fraction containing normal butane and iso-butane,
Saturation liquefied gas containing saturation C3 fraction and C-4-fraction or the C5 fraction containing pentane and isopentane, preferably
For the C-4-fraction containing normal butane and iso-butane or the saturation liquefied gas containing saturation C3 fraction and C-4-fraction.
6. according to the method described in claim 1, wherein, the method for four desorber of the carbon processing includes: by four absorption tower of carbon
It handles obtained liquid phase material to supply to being separated in four desorber of carbon, the number of theoretical plate of four desorber of carbon is 35-45, operation
Pressure is 2.5-3.5MPaG, and tower top temperature is 55-65 DEG C, and bottom temperature is 100-160 DEG C.
7. according to the method described in claim 1, wherein, four desorber of carbon for being back to the recycling of four absorption tower of carbon is handled
To liquid phase be cooled to 5-20 DEG C, be preferably recycled to being back to four absorption tower of carbon after 10-15 DEG C as absorbent.
8. according to the method described in claim 1, wherein, the processing method of the naphtha scrubber includes: by four absorption tower of carbon
It handles obtained gaseous phase materials to supply to contacting it with gasoline absorbent in naphtha scrubber, the number of theoretical plate of naphtha scrubber
For 15-25, operating pressure 2.5-4MPaG, tower top temperature is 20-30 DEG C, and bottom temperature is 25-40 DEG C；
Preferably, the gasoline absorbent is one of gasoline, heavy naphtha and Aromatic raffinate or a variety of, further preferably
It is still more preferably the stable gasoline from refinery for gasoline.
9. according to the method described in claim 1, wherein, the method for the gasoline stabilizer processing includes: by four desorber of carbon
It handles the liquid phase material that obtained fraction liquid phase material and naphtha scrubber are handled to supply to gasoline stabilizer, gasoline
The number of theoretical plate of stabilizer is 25-35, and operating pressure 0.5-1MPaG, tower top temperature is 40-80 DEG C, bottom temperature 120-
150℃。
Preferably, when progress gasoline stablizes processing, fresh gasoline absorbent is supplemented into naphtha scrubber.
10. according to the method described in claim 1, wherein, the method for the condensation process includes: to handle gasoline stabilizer
To gaseous phase materials be cooled to 5-20 DEG C, preferably to 10-15 DEG C；It is further preferred that the condensation process is in gasoline stabilizer
It is carried out in condenser；
The method of the gas-liquid separation processing includes: that the material for obtaining condensation process is supplied to the progress of gasoline stabilizer return tank
Gas-liquid separation, the operating pressure of the gasoline stabilizer return tank are 0.5-1MPaG, and temperature is 5-20 DEG C.
11. a kind of device of recycling refinery saturation dry gas, which is characterized in that the device includes: residue gas compressor, dry gas cooling
Device, four absorption tower of carbon, four desorber of carbon, naphtha scrubber, gasoline stabilizer, gasoline stabilizer condenser and gasoline stabilizer return
Flow tank；
The residue gas compressor, dry gas cooler and four absorption tower of carbon are sequentially communicated according to logistics direction；
The four absorption tower tower top of carbon is connected to naphtha scrubber, and tower reactor is connected to four desorber of carbon；
The naphtha scrubber tower top is connected with fuel gas extraction pipeline, and tower reactor is connected to gasoline stabilizer；
The carbon four desorbs column overhead and is connected with two concentrate gas product of carbon extraction pipeline, and tower reactor pipeline is divided into two, one and carbon
The connection of four absorption towers, another connect with gasoline stabilizer；
The gasoline stabilizer tower top is sequentially communicated gasoline stabilizer condenser and gasoline stabilizer return tank, and tower reactor pipeline is divided into
Two, one connect with naphtha scrubber, and another produces pipeline for extraction gasoline products；
The gasoline stabilizer return tank tower top is connected to residue gas compressor, and tower reactor pipeline is divided into two, and a connection gasoline is steady
Determine tower, another four absorption tower of connection carbon.
12. the device of recycling refinery saturation dry gas according to claim 11, wherein four absorption tower of carbon is connected with newly
Fresh four absorbent of carbon makes up line, and the naphtha scrubber is connected with fresh gasoline absorbent and makes up line.
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| WO2021082825A1 (en) | 2019-10-28 | 2021-05-06 | 中国石油化工股份有限公司 | Method and device for recovering c2-c4 components in methane-containing industrial gas |
| CN115253604A (en) * | 2022-08-09 | 2022-11-01 | 大连理工大学 | Device and method for separating three dry gases rich in carbon and carbon by NMP |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112728869A (en) * | 2019-10-28 | 2021-04-30 | 中国石油化工股份有限公司 | Method and device for recovering three components of carbon two in dry gas |
| WO2021082825A1 (en) | 2019-10-28 | 2021-05-06 | 中国石油化工股份有限公司 | Method and device for recovering c2-c4 components in methane-containing industrial gas |
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