CN102382680A - Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption - Google Patents
Combined technology of catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption Download PDFInfo
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Abstract
The invention discloses a combined technology of a catalytic cracking absorbing stabilizing system and C3 intercooling oil absorption, belonging to the technical field of integration of oil refining and ethylene, and providing a method for recovering dry gas by the combination of the absorbing stabilizing system and the C3 intercooling oil absorption. The method eliminates a desorption column of the absorbing stabilizing system, and avoids the constant circulation of a great amount of ethylene, ethane and liquefied gas in desorption gas between absorption and desorption, thus reducing the load of an absorption column and saving the energy consumption of the desorption column; as coarse C3 in a dethanizing column kettle of an ethylene unit is used as an absorbent, raw material is easy to obtain, and the cost is low; the desorption column of an original C3 oil absorption column for absorbing intercooling oil is eliminated, the constant circulation of a great amount of C2 and C3 in the desorption gas between absorption and desorption is avoided, and an expansion engine and an ice chest are adopted for recovering refrigeration capacity, thus saving consumption of the refrigeration capacity and heat capacity; and the regeneration of a C3 absorbing agent, the demethanation and the separation of the ethylene are all conducted in the ethylene unit, thus fully showing the reciprocity of the oil refining and ethylene, and being reasonable in flow.
Description
Technical field
The present invention relates to the combination process that cold oil absorbs in a kind of absorption-stabilization system by catalytic cracking and the carbon three, say further, relate to the Technology of the oil refining ethene combination that cold oil absorbs in a kind of absorbing-stabilizing system and the carbon three.
Background technology
The combination of refining process and ethylene process process is to realize obtaining the maximum communications and transportation fuel and the output of ethylene raw with the crude oil input of minimum, thus the important behave that realization economizes on resources, increases economic efficiency.The integrated selection that is inevitable of oil refining process and ethylene process design.
The by-product of refining process and ethylene process process supplies reciprocity very strong mutually.Ethylene raw has from the virgin naphtha of refinery and the tops of reformation, the light naphthar of hydrogen cracking and tail oil, hydrogenation coker gasoline, the liquefied gas lighter hydrocarbons behind the gentle branch of reforming raffinate oil.The methane hydrogen that the ethylene plant is discharged supplies the refinery to make hydrogen feedstock; The cracking hydrogenated gasoline raffinated oil supply refinery's reformer to make raw material; Send refinery to produce MTBE the C4 after the divinyl extracting,, remove the C4 separation and Extraction butene-1 behind the iso-butylene as the gasoline octane rating blend component.
The gas separating technology of refining process and ethylene process process also has very strong reciprocity, if rationally utilize, can improve organic efficiency and practice thrift initial cost.The catalytic cracking of refinery absorbs has same attribute stable the separation with the splitting gas of ethylene unit with gas fractionation, if with these technological process combinations, consider as a whole, can reduce investment, improves ethylene recovery efficient.
CCU is one of device of China's most important heavy crude fraction lighting.It is made up of reaction-regeneration system, main fractionating system and absorbing-stabilizing system three parts.The task of fractionating system is to cool off the reaction product oil vapour mixture that reaction-regeneration system comes, and separates into various products, and fractionating system comprises separation column, product stripping tower, each stage casing reflux heat recovery system, and enough heats is provided for absorbing-stabilizing system.The design of the absorption-stabilization system by catalytic cracking of refinery at present is components such as the C3 that is dissolved with in gasoline that rich gas is contained, liquefied gas and lighter component and the raw gasline, C4, separates into dry gas, liquefied gas and stable gasoline.
The typical absorption stabilizing apparatus of refinery mainly is made up of absorption tower, desorption tower, reabsorber and stabilizer tower all the people present tower at present, sees Fig. 1.Compression rich gas 101; With the stripping gas 107 of rich absorbent oil at the bottom of 3 towers of absorption tower 106 and desorption tower 4 cats head after supercooler 1 cooling; Get into vapor-liquid separation tank 2 and carry out vapor-liquid separation; Gas phase gets at the bottom of 3 towers of absorption tower, and liquid phase is squeezed into desorption tower 4 top fed, and the deethanizing gasoline 112 heat exchange rear sections that the stable gasoline 115 that comes out from gasoline stabilizer 6 tower stills comes out at the bottom of with the desorb Tata get into the top, absorption tower as replenishing absorption agent 103 with raw gasline 102.The absorption tower ejects the lean gas 104 that comes and gets at the bottom of reabsorber 5 towers, and solar oil 109 conducts absorption agent again get into the reabsorber top with the component more than the C3 in the further absorption lean gas.Deethanizing gasoline 112 at the bottom of the desorption tower; With getting into gasoline stabilizer 6 after the waste heating of stable gasoline 115; Gasoline stabilizer ejects liquefied gas 114, goes out device as product, and the stable gasoline 115 that comes out from the tower still carries out heat exchange with deethanizing gasoline 112 earlier; One is as replenishing absorption agent 103 after overcooling then, and another strand goes out device as gasoline products 116.
The general characteristics of China's oil refining enterprise are that catalytic cracking proportion is bigger in the secondary processing device; Built in China has the over one hundred cover of CCU according to statistics; Existing CCU yearly capacity 100Mt; The about 4.14Mt of catalytic cracked dry gas that produced in 2008, so the plant catalytic dry gas amount is bigger, the present major part of these dry gas all acts as a fuel and burns.Owing to contain ethene, propylene and ethane, the propane component of significant proportion in these dry gas, wherein contain alkane components 6% (wt) such as ethene 40% (wt), ethane 40% (wt), propylene 6% (wt), butylene 2% (wt), propane and butane, hydrogen 6% (wt).If can be with the CO in the dry gas
2, H
2S, O
2And Impurity removal such as nitrogenous compound and the methane that reclaims in the dry gas are used as hydrogen feedstock with hydrogen; Simultaneously ethene, propylene and lighter hydrocarbons enrichments such as ethane, propane in the dry gas are got up; Without pyrolyzer, directly get into the ethylene unit separation system, just can separate obtaining a considerable amount of ethene and propylene; And remaining ethane, propane lighter hydrocarbons are circulated to pyrolyzer with ethane, the propane of splitting gas Separation and Recovery, can obtain more ethene and propylene again.Thereby the dry gas of the low value that can only burn as fuel has become ethene, propylene and high-quality cracking stock and the best hydrogen feedstock of high value.If catalytic cracked dry gas reclaims the lighter hydrocarbons technology and popularizes in an all-round way at home, can practice thrift the lightweight oil 4.15Mt that is used to produce ethene every year, can the create beneficial result over ten billion Yuan.Therefore from oil refinery dry gas, reclaim the huge breach that ethene can suitably remedy domestic ethene supply, replenish as the useful of domestic ethylene production.This is that the performance oil-refining chemical is integrated, optimizes ethylene raw, increases ethylene yield, reduces a good measure of ethene cost.
The method that from plant catalytic dry gas, reclaims ethene at present mainly contains separation by deep refrigeration, middle cold oil absorption process, Separation by Complexation method, pressure swing adsorption process etc., and the whole bag of tricks differs from one another.The separation by deep refrigeration technical maturity, the ethylene recovery rate is high, but investment is big, and it is higher to be used for rare ethylene recovery energy consumption; The Separation by Complexation method, the ethylene recovery rate is higher, but strict to impurities in raw materials, and the pre-treatment expense is higher, needs special complexed absorption agent; Pressure swing adsorption process is simple to operate, and energy consumption is lower, but product purity is low, and the ethylene recovery rate is low, and floor space is big.
Middle cold oil absorption process mainly is to utilize absorption agent that the different solubility of each component in the gas is come separating gas mixture; The general absorption agent that utilizes earlier absorbs C2 and the above heavy constituent of C2; Isolate non-condensable gasess such as methane, hydrogen, use each component in the agent of rectification method separate absorbent again.This method has characteristics such as small scale, flexibility is strong, investment cost is low, can be used for from splitting gas, separating alkene, from Sweet natural gas, reclaims technology such as lighter hydrocarbons.Middle cold oil absorption process can be used for the recovery of low-concentration ethane in the catalytic cracked dry gas, but the loss of cold oil absorption technique absorption agent is big in the traditional conventional, the ethylene recovery rate is lower, and the recovery has only about 85% usually.
CN 1640992 proposed a kind ofly to be applicable to from associated gas or Sweet natural gas and to reclaim liquefied gas to install the refrigeration oil absorption process that self-produced stable light hydrocarbon is an absorption agent, and the C3 yield recovery technology of having relatively high expectations.Adopt the absorption process of this refrigeration oil, can obtain higher light hydrocarbon recovery rate, and technology be simple with less absorption agent, energy consumption is lower, better economic benefit.But this method only is applicable to from associated gas or Sweet natural gas and reclaims liquefied gas, can not reclaim the C2 cut, can't be used for the recovery of plant catalytic dry gas.
CN 1414067 proposed a kind of after the shallow cold technology of Sweet natural gas grafting oil absorption technique, thereby improve the method for light hydrocarbon recovery rate.This method makes gains get in the secondary triphase separator after the shallow cold technology of Sweet natural gas to carry out gas-liquid separation, makes bottom that gas gets into the absorption tower and absorption agent carry out gas-liquid and exchanges and obtain reclaiming behind C3, the C4 component; Liquid mixes in the back entering desorption tower with the interior lighter hydrocarbons of secondary triphase separator deviates from methane and ethane, and taking off of formation reclaimed after imbibition entering Analytic Tower cuts out C3, C4 component.This method can improve the light hydrocarbon recovery rate in the Sweet natural gas, increases lighter hydrocarbons output.But this method only is applicable to and from Sweet natural gas, reclaims lighter hydrocarbons, and is not suitable for the recovery of plant catalytic dry gas.
US 5502971 discloses a kind of C2 of recovery and has reached the more low-pressure low-temperature technology of heavy hydrocarbons, is applicable to the recovery of oil refinery dry gas.This technology has been cancelled traditional high pressure scheme, changes and adopts low-voltage technology, and recovered temperature just can remain on the temperature that the nitric acid resin generates like this, has avoided dangerous potential possibility, can also keep higher olefin yields simultaneously.This process using the low pressure scheme, temperature is low to reach-100 ℃, belongs to a kind of of deep cooling process for separating, invests greatlyyer, energy consumption is higher.
US 6308532 has proposed a kind of technology that from oil refinery dry gas, reclaims ethene and propylene; This technology comprises that from the absorption tower still extracts C3, C4, C5, C6 liquid out and part tower bottoms phase materials is circulated to cat head; Thereby keep the freezing temp of overhead condenser to be not less than-95 ℃, in the absorption tower, be rich in propylene or ethene-propylene zone simultaneously and extract the gas phase side line out.Although this technology is circulated to cat head with part tower still material and was unlikely low to keep tower top temperature, tower top temperature is still low to reach-95 ℃, still belongs to a kind of of deep cooling process for separating, and therefore investment is bigger, and energy consumption is higher.
CN 1800308 and CN 101371966 have proposed a kind of pressure swing adsorption technique from refinery dry gas recovery ethene and hydrogen, and this technological core is a transformation absorption method of enrichment.Catalysis drying gas needs through strict cleaning section to remove the impurity in the dry gas, desulfurization again, decarburization, hydrogenation, drying before sending transformation fractionation by adsorption device.This method needs a plurality of adsorption tower combine operationss, separates concentrated lighter hydrocarbons through the continuous switching between absorption, the desorption.Problems such as a typical pressure-swing absorption apparatus needs 10-16 platform adsorption tower, and each adsorption tower is all through absorption, displacement, contrary step repeatable operation such as put, find time, boost, and this method exists facility investment high, and floor space is big.
Therefore,, can absorption-stabilization system by catalytic cracking, dry gas be reclaimed and the ethene flow process considered as a whole, develop a kind of Technology that ethene makes up of refining oil for energy consumption that reduces existing absorbing-stabilizing system and the ethylene recovery rate that improves oil refinery dry gas.
Summary of the invention
For energy consumption that reduces existing absorbing-stabilizing system and the ethylene recovery rate that improves oil refinery dry gas, the present invention proposes cold oil absorption COMBINED PROCESS in a kind of absorption-stabilization system by catalytic cracking and the carbon three.Concrete technical scheme is following.
The COMBINED PROCESS that cold oil absorbs in absorption-stabilization system by catalytic cracking of the present invention and the carbon three comprises following steps:
(1) catalytic cracking absorbs stable: rich absorption liquid mixes at the bottom of will compressing rich gas and absorbing Tata; Be cooled to 35～45 ℃ through water cooler; Air inlet liquid separating tank, the gas that goes out from knockout drum gets into the absorption tower, in the absorption tower, absorbs the liquefied gas (C3, C4) in the rich gas with raw gasline and additional absorption agent (stable gasoline); From absorbing the lean gas entering reabsorber that cat head is discharged, absorb the gasoline light constituent in the lean gas with solar oil.The liquid of telling from knockout drum and the laggard gasoline stabilizer of stable gasoline heat exchange of gasoline stabilizer still carry out fractionation; Liquefied gas is extracted out from the gasoline stabilizer side line; Behind the liquid heat exchange that the stable gasoline of gasoline stabilizer still and gasoline knockout drum go out a part as a supplement absorbent get into the absorption tower; A part goes out the battery limit (BL) as the stable gasoline product; The dry gas of discharging from the gasoline stabilizer top mixes with the dry gas of discharging from the reabsorber top; Successively through amine wash, after alkali cleaning and the drying; Get into compressor and boost to 3.5～4.5MPa, cold carbon three oil-absorption towers in sending into;
(2) cold carbon three oil absorb in: from the dry gas of compressor outlet after water-cooled; Successively with in the flash gas of methane hydrogen tail gas, low pressure separation pot of cold carbon three oil-absorption towers change cold after; Be chilled to-30～-35 ℃ with refrigerant; Cold carbon three oil-absorption towers in the entering, the thick carbon of sending here with ethylene unit three (deethanizing tower bottoms) absorbs ethene, ethane in the dry gas.In the rich solution that is rich in carbon two of cold carbon three oil-absorption tower stills, through change cold after, return the demethanizing tower of ethylene unit.
In in cold carbon three oil-absorption towers unabsorbed hydrogen, nitrogen, methane and therefrom cold carbon three oil-absorption towers of the small amount of carbon three absorption agents top of carrying secretly discharge; Get into methane hydrogen that ice chest and decompressor export change cold after; Get into the high pressure separating tank, carry out gas-liquid separation.Be back to top, absorption tower from the isolated liquid phase of high pressure separating tank as absorption agent, gas gets into decompressor and freezes.The gas of decompressor outlet gets into low pressure separation pot and carries out gas-liquid separation, and the liquid phase of low pressure separation pot is returned the residue gas compressor inlet after cold is reclaimed in gasification, after reclaiming cold, go the pressure-swing absorption apparatus recover hydrogen from the isolated gas of low pressure separation pot.
In step (1), the number of theoretical plate on said absorption tower is preferably 8～20, and working pressure is preferably 1.2～1.5MPa; 1.35MPa more preferably, tower top temperature is preferably 40 ℃～45 ℃, more preferably 42 ℃; Tower still temperature is preferably 43～48 ℃, more preferably 4 ℃.1～2 side cooler of preferred employing remains between 4 ℃～48 ℃ the temperature of absorber portion in the tower.
In step (1), the number of theoretical plate of said reabsorber is preferably 6～15, and working pressure is preferably 1.1～1.4MPa; 1.35MPa more preferably, tower top temperature is preferably 4 ℃～50 ℃, more preferably 45 ℃; Tower still temperature is preferably 52～58 ℃, more preferably 55 ℃.
In step (1), the number of theoretical plate of said gasoline stabilizer is preferably 30～40, and working pressure is preferably 0.8～1.2MPa; 1.0MPa more preferably, tower top temperature is preferably-20 ℃～-30 ℃, more preferably-25 ℃; Tower still temperature is preferably 160～180 ℃, more preferably 170 ℃.
In step (1), the dry gas of discharging from gasoline stabilizer top is with after the dry gas of discharging from the reabsorber top mixes, and entering amine is washed tower, soda-wash tower removes sour gas.Said sour gas for example is H
2S, CO
2Deng.Amine is washed, alkali cleaning removes sour gas because methods such as transformation absorption, low temperature separation process also need be carried out; Therefore the concrete processing condition to this step do not have special qualification, and those skilled in the art can confirm its concrete operations condition and method suitably according to other method.
If desired, method of the present invention also comprises drying and purifying step: water and trace impurity in the dry gas that obtains in the step (1) are removed.With above-mentioned to remove the sour gas step the same; Also need carry out drying and purifying step in methods such as transformation absorption, low temperature separation processs; Therefore the concrete processing condition to this step do not have special qualification, and those skilled in the art can confirm its concrete operations condition and method suitably according to other method.For instance, can adopt the 3A molecular sieve to remove moisture and trace impurity as siccative; Adopt the protection bed to remove trace impurities such as arsenic.
In step (1); The pressure of the catalysis drying gas after super-dry and purifying step generally is about 0.7～0.9MPa; Generally need improve the pressure of catalysis drying gas step by step, although the hop count of compression is not had special qualification, two sections compressions of general preferred employing; From the angle analysis of economic benefit, it is more rational adopting two sections compressions.To bring up to 3.0～4.0Mpa through two sections compression pressures through the catalysis drying gas after super-dry and the purifying step.
In step (2); The number of theoretical plate of cold carbon three oil-absorption towers is preferably 8～20 in said, and working pressure is preferably 3.2～3.8MPa, more preferably 3.5MPa; Tower top temperature is preferably-35 ℃～-25 ℃; More preferably-26 ℃, tower still temperature is preferably-35 ℃～-25 ℃ ℃, more preferably-28 ℃.
The COMBINED PROCESS that cold oil absorbs in absorption-stabilization system by catalytic cracking of the present invention and the carbon three has following characteristics:
(1) cancels the desorption tower of absorbing-stabilizing system, avoided the constantly circulation of ground between absorption and desorption of a large amount of ethene, ethane and the liquefied gas in the stripping gas, thereby reduced the load on absorption tower, the energy consumption of having saved desorption tower;
(2) with the thick carbon three of the deethanizing column still of ethylene unit as absorption agent, raw material obtains easily, and is with low cost;
(3) cancelled former in the desorption tower of carbon three oil-absorption towers that absorb of cold oil, avoided carbon two and carbon three constantly circulation of ground between absorption and desorption in a large amount of stripping gass, adopt decompressor and ice chest recovery cold, saved cold and heat exhaustion;
(4) regeneration of carbon three absorption agents, demethanizing, ethene separation are all carried out at ethylene unit, have demonstrated fully the reciprocity of oil refining and ethene;
(5) the ethylene recovery rate is high, can reach more than 95.5%.
Description of drawings
Fig. 1 is the typical absorption stabilizing apparatus of present refinery, mainly is made up of absorption tower, desorption tower, reabsorber and stabilizer tower all the people present tower.
Fig. 2 is the combination process schematic flow sheet that cold oil absorbs in absorption-stabilization system by catalytic cracking of the present invention and the carbon three.
The 1-water cooler; The 2-knockout drum; The 3-absorption tower; The 4-reabsorber; The 5-gasoline stabilizer; 6-stable gasoline and stable gasoline tower feed exchanger; 7-amine is washed tower; The 8-soda-wash tower; The 9-moisture eliminator; The 10-residue gas compressor; 11-dry gas and low pressure separation pot liquid phase interchanger; The 12-ice chest; 13-high pressure separating tank; The 14-decompressor; The 15-low pressure separation pot; Water cooler before cold carbon three oil-absorption towers during the 16-dry gas advances; Cold carbon three oil-absorption towers among the 17-; The 18-ice chest; 19-methane hydrogen tail gas and dry gas interchanger; Thick carbon three water coolers of 20-; The thick carbon of 21-three with in liquid phase interchanger at the bottom of the cold carbon three oil-absorption tower towers;
101-compresses rich gas; The 102-raw gasline; 103-knockout drum gas phase; Rich absorption liquid at the bottom of the 104-absorption tower; 105-knockout drum liquid phase; 106-replenishes absorption agent; It is stingy that 107-absorbs cat head; The 108-solar oil; 109-reabsorber top dry gas; The rich diesel oil of 110-; The charging of 111-gasoline stabilizer; 112-gasoline stabilizer still stable gasoline; 113-stable gasoline product; 114-gasoline stabilizer top dry gas; The 115-liquefied gas; 116-amine soda is washed the back dry gas; 117-compresses dry gas; Cold carbon three oil-absorption tower dry gas chargings among the 118-; 119-high pressure separating tank liquid phase; Cold carbon three oil-absorption towers in the cold carbon three absorption agent chargings among the 120-; The thick carbon three of 122-; 123-methane hydrogen.
Embodiment
Below in conjunction with embodiment, further specify the present invention, but the present invention is not limited to embodiment.
The mole composition of certain oil plant catalytic cracking compression rich gas sees Table 1.Absorption is stablized the Engler distillation data of used raw gasline and solar oil and is seen table 2.
Mix with rich absorption liquid 104 at the bottom of the absorption tower from the compression rich gas 101 of rich gas compressor; Be cooled to 40 ℃ through water cooler 1; Get into knockout drum 2 and carry out equilibrium separation; The service temperature of vapor-liquid separation tank is 40 ℃, and working pressure is 1.45MPa, from 3 bottoms, gas phase 103 entering absorption towers that knockout drum comes out.The number of theoretical plate on absorption tower is preferably 12; Working pressure is 1.37MPa; Tower top temperature is 43.2 ℃, and tower still temperature is 45.2 ℃, in the absorption tower, gets into the top, absorption tower with raw gasline 102 and additional absorption agent 106 as absorption agent; Absorb C3, C4 component in the rich gas, replenishing absorption agent is the part from the stable gasoline of gasoline stabilizer 5 tower stills.From absorbing the lean gas 107 entering reabsorbers 4 that cat head is discharged, the number of theoretical plate of reabsorber is preferably 10, and working pressure is 1.35MPa; Tower top temperature is 45.8 ℃; Tower still temperature is 54.8 ℃, and solar oil 108 gets into reabsorber 4 tops, absorbs the gasoline component in the lean gas; Go out rich diesel oil 110 from reabsorber 4 bottoms and go out the battery limit (BL), discharge dry gas 109 from the reabsorber top.Get into the 20th block of column plate of gasoline stabilizer after the liquid of telling from knockout drum 105 and stable gasoline 112 heat exchange of gasoline stabilizer still and carry out fractionation; The number of theoretical plate of gasoline stabilizer is preferably 36; Working pressure is 1.0MPa, and tower top temperature is-26.7 ℃, and tower still temperature is 170.1 ℃; Liquefied gas 115 is extracted out from the 10th block of column plate of gasoline stabilizer side line; A part is as replenishing absorption agent 106 entering absorption towers after liquid 105 heat exchange that the stable gasoline 112 and the gasoline separating tank of gasoline stabilizer still goes out, and a part goes out the battery limit (BL) as stable gasoline product 113, and the dry gas 114 of discharging from the gasoline stabilizer top mixes with the dry gas 109 of discharging from the reabsorber top.C4 content is less than prescribed value in the stable gasoline of control gasoline stabilizer still, and the gasoline stabilizer top adopts cryogen to carry out condensation.
After logistics 109 and 114 mixing dry gas are washed tower 7, soda-wash tower 8 and dry cleaner 9 through amine successively; Get into residue gas compressor 10 and boost to 3.8MPa through two sections compressions; From the dry gas of compressor outlet behind watercooler, successively with in the liquid phase boil-off gas of methane hydrogen tail gas, low pressure separation pot 15 of cold carbon three oil-absorption towers 17 change cold after, be chilled to-3 ℃ with cryogen in the water cooler 16 before cold carbon three oil-absorption towers in the entering; Cold carbon three oil-absorption towers bottom in getting into then; In the number of theoretical plate of cold carbon three oil-absorption towers be preferably 10, working pressure is 3.5MPa, tower top temperature is-25.6 ℃; Tower still temperature is-28.8 ℃; The thick carbon of sending here with ethylene unit 3 122 absorbs ethene, ethane in the dry gas as cold carbon three oil-absorption tower tops in the absorption agent entering, and thick carbon three is the tower bottoms from the ethylene unit deethanizing column, and its mole composition is seen table 3.In the rich solution 121 that is rich in carbon two components at the bottom of cold carbon three oil-absorption towers, through with thick carbon three change cold after, return the demethanizing tower of ethylene unit, and then isolate ethene and ethane.
In in cold carbon three oil-absorption towers unabsorbed hydrogen, nitrogen, methane and therefrom cold carbon three oil-absorption towers of the small amount of carbon three absorption agents top of carrying secretly discharge; The methane hydrogen that gets into ice chest 12 and decompressor 14 outlets change cold after; Get into high pressure separating tank 13; High pressure separating tank working pressure is 3.5MPa, enters to the 4th block of column plate in absorption tower from the isolated liquid phase 119 of high pressure separating tank as absorption agent, gets into decompressor from the isolated gas of high pressure separating tank and freezes.The decompressor exit gas gets into low pressure separation pot 15 and carries out gas-liquid separation; The low pressure separation pot working pressure is 1.0MPa; The liquid phase of low pressure separation pot is returned the residue gas compressor inlet after cold is reclaimed in gasification, after reclaiming cold, remove pressure-swing absorption apparatus recover hydrogen and methane from the isolated gas of low pressure separation pot.
Table 1 catalytic cracking rich gas mole is formed
| Component | Mole is formed | Component | Mole is formed |
| H 2 | 0.2475 | Trimethylmethane | 0.0411 |
| Air | 0.0918 | Normal butane | 0.0103 |
| CO 2 | 0.0108 | 1-C 4H 8 | 0.0502 |
| H 2S | 0.0094 | Suitable-butene-2 | 0.0191 |
| CH 4 | 0.1203 | Instead-butene-2 | 0.0233 |
| C 2H 6 | 0.0572 | Iso-pentane | 0.0233 |
| C 2H 4 | 0.0609 | Skellysolve A | 0.0578 |
| C 3H 6 | 0.1293 | Normal hexane | 0.0225 |
| C 3H 8 | 0.0252 |
Table 2 raw gasline and solar oil Engler distillation data
| Project | Raw gasline | Solar oil |
| Proportion | 0.7036 | 0.8847 |
| Over point (℃) | 34 | 184 |
| 10％ | 58 | 240 |
| 50％ | 108 | 287 |
| 90％ | 182 | 346 |
| Final boiling point (℃) | 200 | 356 |
The thick three moles of compositions of carbon of table 3
| Component | Mole is formed | Component | Mole is formed |
| C 2H 6 | 0.0004 | C 4H 8 | 0.0873 |
| C 2H 4 | 0.0000 | C 4H 6 | 0.1192 |
| C 3H 6 | 0.7036 | C 5H 10 | 0.0256 |
| C 3H 8 | 0.0266 | C 6H 14 | 0.0019 |
| C 3H 4 | 0.0257 | C 6H 6 | 0.0069 |
| C 4H 10 | 0.0025 | C 7H 8 | 0.0003 |
In the present embodiment, the recovery of ethene is 95.54%.
Claims (8)
1. the combination process that cold oil absorbs in absorption-stabilization system by catalytic cracking and the carbon three comprises following steps:
(1) catalytic cracking absorbs stable
Absorption-stabilization system by catalytic cracking comprises water cooler, knockout drum, absorption tower, reabsorber, gasoline stabilizer, stable gasoline and stable gasoline tower feed exchanger
The catalytic cracking absorption stabilizing process: rich absorption liquid mixes at the bottom of will compressing rich gas and absorbing Tata; Be cooled to 35～45 ℃ through cooler; Air inlet liquid knockout drum; The gas that goes out from knockout drum gets into the absorption tower; In the absorption tower, absorb the liquefied gas in the rich gas with raw gasoline and additional absorbent; From absorbing the lean gas entering reabsorber that cat head is discharged, absorb the gasoline light component in the lean gas with light diesel fuel; The liquid of telling from knockout drum and the laggard gasoline stabilizer of stable gasoline heat exchange of gasoline stabilizer still carry out fractionation; Liquefied gas is extracted out from the gasoline stabilizer side line; Behind the liquid heat exchange that the stable gasoline of gasoline stabilizer still and gasoline knockout drum go out a part as a supplement absorbent get into the absorption tower; A part goes out the battery limit (BL) as the stable gasoline product; The dry gas of discharging from the gasoline stabilizer top mixes with the dry gas of discharging from the reabsorber top; Successively through amine wash, after alkali cleaning and the drying; Get into compressor and boost to 3.5～4.5MPa, cold carbon three oil-absorption towers in sending into;
(2) cold carbon three oil absorb in
In cold carbon three oily absorption systems comprise amine wash tower, soda-wash tower, moisture eliminator, residue gas compressor, dry gas and low pressure separation pot liquid phase interchanger, ice chest, high pressure separating tank, decompressor, low pressure separation pot, dry gas advance in water cooler before cold carbon three oil-absorption towers, in cold carbon three oil-absorption towers, ice chest, methane hydrogen tail gas and dry gas interchanger, thick carbon three water coolers, thick carbon three and in liquid phase interchanger at the bottom of the cold carbon three oil-absorption tower towers
In cold carbon three oily absorption techniques: from the dry gas of compressor outlet after water-cooled; Successively with in the flash gas of methane hydrogen tail gas, low pressure separation pot of cold carbon three oil-absorption towers change cold after; Be chilled to-30～-3 ℃ with refrigerant; Cold carbon three oil-absorption towers in the entering, ethene, ethane that the thick carbon of sending here with ethylene unit three absorbs in the dry gas; In the rich solution that is rich in carbon two of cold carbon three oil-absorption tower stills, through change cold after, return the demethanizing tower of ethylene unit
In in cold carbon three oil-absorption towers unabsorbed hydrogen, nitrogen, methane and therefrom cold carbon three oil-absorption towers of the small amount of carbon three absorption agents top of carrying secretly discharge; Get into methane hydrogen that ice chest and decompressor export change cold after; Get into the high pressure separating tank; Carry out gas-liquid separation: be back to top, absorption tower from the isolated liquid phase of high pressure separating tank as absorption agent, gas gets into decompressor and freezes; The gas of decompressor outlet gets into low pressure separation pot and carries out gas-liquid separation, and the liquid phase of low pressure separation pot is returned the residue gas compressor inlet after cold is reclaimed in gasification, after reclaiming cold, go the pressure-swing absorption apparatus recover hydrogen from the isolated gas of low pressure separation pot.
2. combination process according to claim 1, in step (1), the number of theoretical plate on said absorption tower is 8～20, and working pressure is 1.2～1.5MPa, and tower top temperature is 4 ℃～℃, and tower still temperature is 43～4 ℃.
3. combination process according to claim 2, in step (1), the working pressure on said absorption tower is 135MPa, and tower top temperature is 4 ℃, and tower still temperature is 4 ℃.
4. combination process according to claim 1 in step (1), adopts 1～2 side cooler in the said absorption tower, the temperature of absorber portion remains between 4 ℃～4 ℃.
5. combination process according to claim 1, in step (1), the number of theoretical plate of said reabsorber is 6～15, and working pressure is 1.1～1.4MPa, and tower top temperature is 4 ℃～℃, and tower still temperature is 52～5 ℃.
6. combination process according to claim 5, in step (1), the working pressure of said reabsorber is 1.35MPa, and tower top temperature is 4 ℃, and tower still temperature is 5 ℃.
7. combination process according to claim 1, in step (1), the number of theoretical plate of said gasoline stabilizer is 30～40, and working pressure is 0.8～1.2MPa, and tower top temperature is-20 ℃～-30 ℃, and tower still temperature is 160～180 ℃.
8. combination process according to claim 7, in step (1), the working pressure of said gasoline stabilizer is 1.0MPa, and tower top temperature is-25 ℃, and tower still temperature is 170 ℃.
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