CN102925213B - Treatment method for light hydrocarbon-containing petrochemical industry gas - Google Patents
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- CN102925213B CN102925213B CN201110227179.0A CN201110227179A CN102925213B CN 102925213 B CN102925213 B CN 102925213B CN 201110227179 A CN201110227179 A CN 201110227179A CN 102925213 B CN102925213 B CN 102925213B
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Abstract
The present invention provides a treatment method for light hydrocarbon-containing petrochemical industry gas, wherein the light hydrocarbon-containing petrochemical industry gas contains hydrocarbon having carbon atom number of 1-4. The method comprises that: the light hydrocarbon-containing petrochemical industry gas contacts a first absorption agent, such that the hydrocarbon having a carbon atom number of more than or equal to 2 is absorbed by the first absorption agent, and content of the hydrocarbon having a carbon atom number of 2 is reduced to less than 3 mol% through the contact condition to obtain a first rich absorption liquid and first lean gas; and the first rich absorption liquid is subjected to desorption in a desorption tower to separate ethane-rich gas. With the treatment method, C2 fraction recovery rate of the common hydrocarbon-containing petrochemical industry gas having a C2 component content of more than 20 mol% in a refinement enterprise can be more than 90%.
Description
Technical field
The present invention relates to a kind for the treatment of process containing lighter hydrocarbons petrochemical complex gas.
Background technology
Petrochemical complex is a very huge commercial run, needs to be carried out by hundreds and thousands of kinds of materials transforming and being separated the product obtaining high value.In the processes processes such as atmospheric and vacuum distillation, catalytic cracking, cracking, coking, catalytic reforming, isomerization, the gas that capital by-product is a large amount of, wherein just containing light hydrocarbon material such as hydrogen, nitrogen, methane, C2 lighter hydrocarbons (also referred to as carbon two), liquefied petroleum gas (LPG), these gas grosses exceed that total amount always processed by oil 5%.And these byproducts are mostly the somes in desired raw material in petrochemical process production process, particularly hydrogen, carbon two, liquefied petroleum gas (LPG) etc. are the raw materials that the price that needs in petrochemical production process is higher, recovery large-scale popularization and the application in the industry of liquefied petroleum gas (LPG) and hydrogen, technique is quite ripe---and cryogenic condensation is separated, turning oil absorbs the widespread uses such as Ethylene recov liquefied oil gas technology, gas film and pressure-variable adsorption separating and reclaiming hydrogen.
Carbon two in petrochemical complex by-product gas is raw materials of a kind of producing ethylene by cracking of high-quality, with other cracking stocks as liquefied petroleum gas (LPG), petroleum naphtha are compared with diesel oil, has the advantages such as per pass conversion is high, yield of ethene is high, production energy consumption is low.According to the production status of current China refinery, ethane content in atmospheric and vacuum distillation overhead gas is usually more than 20 % by mole, in catalytic cracked dry gas, ethane/ethylene content is more than 25 % by mole, ethane/ethylene content in coking dry gas is more than 20 % by mole, C-2-fraction content in other hydrogenation gas have also exceeded 25 % by mole after hydrogen recovery, obviously, ethylene industry raw material abundant in containing in hydrocarbonaceous petrochemical complex gas.According to the statistics of subordinate S & W company of Shaw group of the U.S., ten million ton of refining & chemical industry integration enterprise can auxiliary construction scale be the ethane cracking device of 160,000 tons/year.China in 2010 oil refining scale reaches 7.5 hundred million tons/year, if effectively reclaim C-2-fraction wherein, reaches the level of comprehensive utilization of external Integrated Refinery And Petrochemical, can output ethylene production raw material more than 1,200 ten thousand tons.China Petrochemical Industry, PetroChina Company Limited. and CNOOC subordinate ten-million-ton scale oil refining base reach 15, wherein the crude oil comprehensive working ability of Sinopec Zhenghai refinery branch office reaches 2,000 ten thousand tons/year, rely on these large-scale oil refining bases, effectively can carry out the work of carbon two component Collection and utilization.From hydrocarbonaceous petrochemical complex gas, reclaim carbon two component become the following effective way increasing the performance of enterprises, improve enterprise competitiveness as industrial chemicals.
Sweet natural gas and associated gas are the main sources of industrial ethane, carry out the low temperature that throttling expansion or turbine expansion can obtain less than-100 DEG C, therefore often adopt cold separation technology to high-pressure natural gas and associated gas.The working pressure of most of hydrocarbonaceous petrochemical complex gas is at below 2.0MPa, do not possess by the ability obtaining low temperature that expands, and adopt refrigerator to provide deep cooling cold to cause the production energy consumption of ethane higher, be unfavorable for popularization and the development of hydrocarbonaceous petrochemical complex gas recovery ethane.
Comparatively speaking, in Petrochemical Enterprises, the method for absorption and desorption is adopted to be separated lighter hydrocarbons more general, as adopted petroleum naphtha, absorption extraction is carried out to the liquefied petroleum gas (LPG) in ordinary decompression column top gas, catalytic cracking gasoline carries out absorption extraction to the liquefied petroleum gas (LPG) in catalytic cracked dry gas, in the standard configuration of the devices such as catalytic cracking, prolonging just with absorbing-stabilizing system.
What prior art produced in the processes processes such as atmospheric and vacuum distillation, catalytic cracking, cracking, coking, catalytic reforming, isomerization that reclaim contains in the process of lighter hydrocarbons petrochemical complex gas in a large number, carbon two component is not generally separated separately, but be mixed together with other lighter hydrocarbons and directly burn afterwards, cause the C2 lighter hydrocarbons of a large amount of high value to fail effectively to utilize thus.
Summary of the invention
The present invention in order to overcome the above-mentioned defect of prior art, provide a kind of can reclaim respectively C1 and more light constituent, rich ethane gas containing the treatment process of lighter hydrocarbons petrochemical complex gas.
The invention provides a kind for the treatment of process containing lighter hydrocarbons petrochemical complex gas, the described lighter hydrocarbons petrochemical complex gas that contains contains the hydrocarbon that carbonatoms is 1-4, wherein, the method comprises and this being contacted with the first absorption agent containing lighter hydrocarbons petrochemical complex gas, the hydrocarbon of more than C2 is absorbed by the first absorption agent, and the condition of contact makes the content of the hydrocarbon of C2 be reduced to less than 3 % by mole, obtains the first rich absorption liquid and the first lean gas; Described first rich absorption liquid is gone out rich ethane gas through Desorption separation in desorption tower.
Treatment process of the present invention, according to the absorption of different material in absorption agent and the difference being desorbed ability, on the basis of prior art, for atmospheric and vacuum distillation, catalytic cracking, cracking, coking, catalytic reforming, a large amount of the containing in lighter hydrocarbons petrochemical complex gas containing a large amount of C2 that the processes processes such as isomerization produce, the feature of liquefied petroleum gas (LPG) (LPG), utilize hydrogen, methane, the other physical qualitative differences such as ethane, along with heavy constituent is by the difference of absorption agent degree of absorption, by controlling the operating parameters absorbed, control the degree absorbed, then by the desorb in desorption tower of the rich absorption liquid of gained, by controlling the operating parameters of desorb, control the degree of depth of desorb, thus make the desorb in desorption tower of rich ethane gas, thus to realize in desorb overhead gas rich ethane gas out below C1 concentration of component lower than 20 % by mole, C2 component concentration concentration reaches 65 % by mole of the above object, thus make the rich ethane gas separated through hydrogenation unit hydrogenation or refining after can reach standard into ethane cracking furnace.Concrete, by contacting with absorption agent containing lighter hydrocarbons petrochemical complex gas, to absorb the hydrocarbon of more than C2, and make the content of the hydrocarbon of C2 be reduced to less than 3 % by mole, obtain rich absorption liquid and lean gas, then according to the feature of rich absorption liquid, by desorb, rectifying, the recovery respectively of rich ethane gas and C3-C4 light ends fractionation is realized.Method of the present invention, each device ubiquitous (as absorption tower, desorption tower, rectifying tower etc.) in refinery can be made full use of, by carrying out Reasonable adjustment to the operating parameters of each device, realize the recycling of coal mine gas, rich ethane gas and C3-C4 light ends fractionation.
Method of the present invention, to the hydrocarbonaceous petrochemical complex gas of carbon two component concentration common in Petrochemical Enterprises more than 20 % by mole, the rate of recovery of C-2-fraction reaches 90%.
In a word, method of the present invention, all has good recovering effect to most of hydrocarbonaceous petrochemical complex gas, can create significant economic benefit.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the treatment process containing lighter hydrocarbons petrochemical complex gas provided by the invention.
Embodiment
The invention provides a kind for the treatment of process containing lighter hydrocarbons petrochemical complex gas, the described lighter hydrocarbons petrochemical complex gas that contains contains the hydrocarbon that carbonatoms is 1-4, wherein, the method comprises and this being contacted with the first absorption agent containing lighter hydrocarbons petrochemical complex gas, the hydrocarbon of more than C2 is absorbed by the first absorption agent, and the condition of contact makes the content of the hydrocarbon of C2 be reduced to less than 3 % by mole, obtains the first rich absorption liquid and the first lean gas; Described first rich absorption liquid is gone out rich ethane gas through Desorption separation in desorption tower.
According to the present invention, described condition contact with the first absorption agent containing lighter hydrocarbons petrochemical complex gas comprises the temperature of contact, the time of contact and the first absorption agent and contains the volume ratio of lighter hydrocarbons petrochemical complex gas, the selectable range of the temperature of described contact is wider, in order to avoid the too high issuable hydro carbons of temperature absorbs incomplete problem, the problems such as the too low issuable hydrate frozen block of temperature and high energy consumption, the temperature of described contact is generally 10-60 DEG C, is preferably 20-40 DEG C; The time of contact, too short may generation absorbed the problem of balance of not reaching, and in order to avoid the problems referred to above, under preferable case, the time of described contact is at least 20 seconds, was preferably 25-50 second, was especially preferably 25-40 second; Described first absorption agent is excessive with the volume ratio containing lighter hydrocarbons petrochemical complex gas, easily cause liquid flooding and flooding problem, too smallly easily cause dry tower problem, therefore, the present invention first absorption agent is generally 1: 3.5-6.0 with the volume ratio containing lighter hydrocarbons petrochemical complex gas, is preferably 1: 4.5-5.5.
According to the present invention, the described contact containing lighter hydrocarbons petrochemical complex gas and the first absorption agent can be carried out in the device of the condition that they contact existing various can realization, under preferable case, carry out in absorption tower, concrete can comprising the steps: contacts described with the first absorption agent is reverse in the first absorption tower containing lighter hydrocarbons petrochemical complex gas, obtains described first lean gas and described first rich absorption liquid.
Under preferable case, the method also comprises from the first absorption tower recovered overhead first lean gas, and by described first rich absorption liquid with containing lighter hydrocarbons petrochemical complex gas contact after carry out described desorb.Described contact is preferably carried out in the first absorption equilibrium tank.Namely, according to one of the present invention preferred embodiment, in the present invention, be that the described lighter hydrocarbons petrochemical complex gas that contains is contacted with the first absorption agent is reverse in the first absorption tower by described mode contact with the first absorption agent containing lighter hydrocarbons petrochemical complex gas, and from the first absorption tower recovered overhead first lean gas, described treatment process is also included in before Desorption separation goes out rich ethane gas, is contacted by described first rich absorption liquid with containing lighter hydrocarbons petrochemical complex gas in the first absorption equilibrium tank.
Although the described condition contacted in the first absorption equilibrium tank can be carried out with reference to prior art, in order to control in the rich ethane gas that finally obtains, C1 and H
2, N
2, CO, CO
2deng the content of gas, thus the concentration making finally to be separated C2 component in the rich ethane gas obtained is higher, preferably described first rich absorption liquid comprises with the condition contacted in the first absorption equilibrium tank containing lighter hydrocarbons petrochemical complex gas: the temperature of contact is 20-50 DEG C, is more preferably 35-45 DEG C; Time is 10-60s, be more preferably 15-40s, when to control described first rich absorption liquid be aforesaid contact conditions with the condition contacted in the first absorption equilibrium tank containing lighter hydrocarbons petrochemical complex gas, C1 content < 20 % by mole in the rich ethane gas finally obtained can be made.
In desorption tower, the condition of operation generally comprises column bottom temperature and tower top temperature, and the desorption time in desorption tower.Although as long as C1 and being more separated of light constituent and rich ethane gas can be realized through desorb by containing lighter hydrocarbons petrochemical complex gas after the first absorption agent contact, generally, under the prerequisite that can realize object, more few better with drain on manpower and material resources.The present invention is by studying flowage structure and the operating parameters for the treatment of processes, find the column bottom temperature in conservative control desorption tower, the time of tower top temperature and desorb can realize more effective separation, thus isolated rich ethane gas is more prone in follow-up treating processes.
Therefore, under preferable case, the time of desorb is 15-30 second, and the column bottom temperature in desorption tower is 120-160 DEG C, and tower top temperature is 0-50 DEG C.
According to the present invention, under preferable case, method of the present invention also comprises the material after desorb is gone out C3-C4 light ends fractionation through rectifying separation in rectifying tower, obtains stable gasoline.This stable gasoline is preferably partly or entirely used as described first absorption agent.
Described the condition that material after desorb goes out C3-C4 light ends fractionation through rectifying separation in rectifying tower to be comprised: the temperature at the bottom of rectifying tower and the temperature of tower top, the time of rectifying in rectifying tower.The time range of choices of the temperature at the bottom of rectifying tower and the temperature of tower top and rectifying is wider, specifically can decide by the load of rectifying needed for it, under preferable case, temperature at the bottom of rectifying tower is generally 210-240 DEG C, be more preferably 220-230, the temperature of tower top is 0-45 DEG C, more preferably 30-40 DEG C, the rectifying time is 10-50 second, more preferably 20-40 second.
In order to be separated a small amount of C2 component isolated in isolated C3-C4 light ends fractionation from rectifying tower and carry secretly further, method of the present invention also comprises C3-C4 light ends fractionation rectifying separation gone out and carries out gas-liquid separation by the second absorption equilibrium tank, a part in the C3-C4 light ends fractionation that rectifying separation is gone out is as liquefied gas product directly outer row, and a part of isolated gas turns back in desorption tower.
According to the present invention, in order to be separated a small amount of first absorber component of carrying secretly in the first lean gas further, described first lean gas that the method also comprises recovery obtains contacts with the second absorption agent is reverse in second absorption tower, first absorbent contents of carrying secretly in described first lean gas is made to be reduced to less than 0.2 % by mole, obtain the second rich absorption liquid and coal mine gas, the coal mine gas obtained and the second rich absorption liquid are reclaimed respectively.Such as generally make more than 90% of first absorber component of carrying secretly in described first lean gas to be absorbed for coking dry gas, catalytic cracker gas, atmospheric and vacuum tower overhead gas namely can realize making first absorbent contents of carrying secretly in described first lean gas be reduced to less than 0.2 % by mole.
Describedly to comprise reclaiming described first lean gas that obtains with the second absorption agent reverse condition contacted in second absorption tower: the temperature of contact, the volume ratio of time and the second absorption agent and the first lean gas, the temperature of described contact, the volume ratio range of choices of time and the second absorption agent and the first lean gas is all wider, can determine according to the measurer body of required absorption, the temperature of general described contact is 40-60 DEG C, be preferably 40-50 DEG C, the time of described contact is 10-25 second, be preferably 10-15 second, the volume ratio of described second absorption agent and the first lean gas is 1: 15-30, be preferably 1: 15-20.
According to the present invention, the various absorption agents that described first absorption agent, the second absorption agent all can adopt those skilled in the art's routine to use, such as described first absorption agent is generally one or more in raw gasline, treated gasoline, petroleum naphtha, also can be the stable gasoline of gained at the bottom of rectifying tower.Under preferable case, the kind of absorption agent can be selected according to the kind of the hydrocarbonaceous petrochemical complex gas of concrete required process and composition, such as, when the hydrocarbonaceous petrochemical complex gas processed is coking dry gas, catalytic cracker gas, vacuum still overhead gas, raw gasline and/or treated gasoline can be selected as the first absorption agent.In order to make raw material be fully utilized, with save energy, the present invention is especially preferred is partly or entirely used as the first absorption agent by the stable gasoline obtained after described rectifying.Therefore, under preferable case, method of the present invention also comprises partly or entirely to be sent into gained stable gasoline in desorption tower, as the first absorption agent.
As mentioned above, the kind of described second absorption agent also can be selected according to the kind of the hydrocarbonaceous petrochemical complex gas of concrete required process and composition, be generally diesel oil and/or heavy petrol, such as, when the hydrocarbonaceous petrochemical complex gas processed is coking dry gas, catalytic cracker gas, vacuum still overhead gas, diesel oil can be selected to be the second absorption agent.
According to the present invention, described first absorption tower, second absorption tower, desorption tower, rectifying tower, absorption equilibrium tank all can adopt the relative unit such as absorption tower, desorption tower, rectifying tower of the various routines of prior art, the present invention to these devices without particular requirement.
Such as described rectifying tower is generally the rectifying tower comprising condenser, reflux at the bottom of opening for feed, discharge port, tower bottom reboiler, tower, described desorption tower is generally the desorption tower comprising at the bottom of tower heating and overhead condenser, opening for feed, discharge port, described absorption tower, absorption equilibrium tank all can adopt existing various absorption tower, absorption equilibrium tank, do not describe in detail one by one at this.
At the bottom of tower in described absorption tower, desorption tower, rectifying tower, the control of tower top temperature all can adopt the means of prior art to control, and at the bottom of such as, tower in rectifying tower, tower top temperature can be controlled by its tower bottom reboiler and overhead condenser, reflux.
The rectifying time in described soak time in absorption tower, the desorption time in desorption tower, rectifying tower can adopt the means of this area routine to control, such as by regulating and controlling the diameter of the input speed of raw material and tower height, tower, thus the rectifying time in the soak time in absorption tower, the desorption time in desorption tower, rectifying tower can be controlled.
In the present invention, after each component is absorbed, be separated after follow-up variously the known method of prior art all can be adopted to carry out the operational means of each Component seperation, recovery, storage and condition, the present invention is without particular requirement.
Such as, after absorbing, the coal mine gas that obtains can desulfurization afterfire, conventional desulfurizer and condition can realize the object of desulfurization, and for example, in the process of separating the rich ethane gas of sucking-off, by cooling for reflux, C3-C4 light ends fractionation can be condensed into liquid, thus realize being separated of rich ethane gas and C3-C4 light ends fractionation.
Method provided by the invention goes for various hydrocarbonaceous petrochemical complex gas, preferably be applicable to the described total amount containing lighter hydrocarbons petrochemical complex gas as benchmark, carbon two component concentration is 10-50 % by mole, not solidifying component 20-80 % by mole, the hydrocarbonaceous petrochemical complex gas of C3-C4 component 10-40 % by mole, described solidifying component refers to that various boiling point in petrochemical complex is lower than the gas (being generally C1 component and inorganic gas) of 0 DEG C, as one or more in methane, nitrogen, hydrogen, carbon monoxide.In addition, hydrocarbonaceous petrochemical complex gas of the present invention can also containing a small amount of C5, C6 component.Concrete, described can be such as coking dry gas, catalytic cracker gas, vacuum still overhead gas containing lighter hydrocarbons petrochemical complex gas.
Be further detailed a kind of embodiment of method provided by the present invention below in conjunction with Fig. 1, all the other are various, and can to realize embodiments of the present invention all similar, and the present invention repeats no more.
1, after the hydrocarbonaceous petrochemical complex gas after compression contacts with the first rich absorption liquid in the first absorption equilibrium tank V-101, gas phase enters bottom the first absorption tower T-101, reverse contact mass transfer is carried out with the first absorption agent entered from the first absorption tower T-101 tower top, more than C2 component in hydrocarbonaceous petrochemical complex gas is rapidly absorbed into liquid phase, obtain the first rich absorption liquid and the first lean gas, and respectively at the bottom of tower and tower top discharge;
2, enter at the bottom of second absorption tower T-102 tower from first T-101 top, absorption tower the first lean gas out, second absorption agent enters from second absorption tower T-102 top and contacts with the first lean gas is reverse, absorbed by the second absorption agent to make the first absorption agent of carrying secretly in the first lean gas and heavy constituent, the second rich absorption liquid and coal mine gas is obtained after reverse contact, second rich absorption liquid is discharged bottom second absorption tower T-102, transports to follow-up absorption agent refining plant;
3, bottom the first absorption tower T-101 the first rich absorption liquid out enter the first absorption equilibrium tank V-101 contact with hydrocarbonaceous petrochemical complex gas after liquid phase enter into the first desorption tower T-103 from the top of the first desorption tower T-103 and carry out desorb, rich ethane gas (rich ethane gas product) is discharged at the first desorption tower T-103 top;
4, bottom the first desorption tower T-103, liquid out enters rectifying tower T-104 and carries out rectifying, to isolate C3-C4 light ends fractionation, and obtain stable gasoline, this stable gasoline can return the first absorption tower T101 as the first absorption agent, also can arrange outward as stable gasoline product, can also be a part of as the first absorption agent, another part is arranged outward as stable gasoline product.
Below in conjunction with embodiment, the present invention will be described in detail.
In embodiment, stable gasoline (the first absorption agent) and diesel oil (the second absorption agent) composition are in table 1.
Embodiment 1
This embodiment is for illustration of the treatment process containing lighter hydrocarbons petrochemical complex gas provided by the invention.
This embodiment adopts the technical process shown in Fig. 1, wherein hydrocarbonaceous tail gas is coking dry gas (composition is in table 3), raw material add-on is 9.75 tons/hour, be the first absorption agent with raw gasline (composition is in table 1) and the stable gasoline (the two volume ratio is for 1: 5) from rectifying tower T-104, be the second absorption agent (composition is in table 1) with diesel oil, the volume ratio of the first absorption agent and coking dry gas is 1: 3.7, the consumption of the second absorption agent is 140 tons/hour, and in tower, operating parameters is in table 2.The rich ethane gas composition of output is in table 3, and all the other the results are shown in Table 4.
Table 1
Note: consist of the component (if NBP-19 representative bubble point temperature in virtual situation is the hydrocarbons of 19 DEG C) with corresponding bubble point temperature calculated according to the Engler distillation data acquisition pseudo-component method of gasoline or diesel oil.
Table 2
Table 3
| Composition (weight) % | Hydrocarbonaceous tail gas | Rich ethane gas |
| Methane | 25.83 | 11.71 |
| Ethane | 19.97 | 59.03 |
| Ethene | 3.54 | 10.79 |
| Propane | 13.45 | 4.04 |
| Propylene | 7.83 | 2.85 |
| Trimethylmethane | 1.51 | 0.10 |
| Normal butane | 7.68 | 0.07 |
| Iso-pentane | 4.40 | 0.00 |
| Skellysolve A | 0.00 | 0.00 |
| H 2 | 0.47 | 0.05 |
| H 2O | 0.37 | 0.66 |
| H 2S | 5.82 | 7.81 |
| N 2 | 8.14 | 1.32 |
| CO | 0.37 | 0.7 |
| CO 2 | 0.62 | 0.87 |
| kg/h | 9750 | 2956.0 |
| C2 component recovery | 90.00％ |
As can be seen from Table 3, the rate of recovery for the treatment of process C2 component of the present invention is high, and the rate of recovery of C2 component is 90%, and in rich ethane gas, C2 concentration of component reaches more than 69.7 % by weight, this shows, treatment process of the present invention has good industrial utility value.
Claims (13)
1. the treatment process containing lighter hydrocarbons petrochemical complex gas, the described lighter hydrocarbons petrochemical complex gas that contains contains the hydrocarbon that carbonatoms is 1-4, it is characterized in that, the method comprises and this being contacted with the first absorption agent containing lighter hydrocarbons petrochemical complex gas, the hydrocarbon of more than C2 is absorbed by the first absorption agent, and the condition of contact makes the content of the hydrocarbon of C2 be reduced to less than 3 % by mole, obtains the first rich absorption liquid and the first lean gas; Described first rich absorption liquid is gone out rich ethane gas through Desorption separation in desorption tower; Wherein, the temperature that described condition contact with the first absorption agent containing lighter hydrocarbons petrochemical complex gas comprises contact is 10-60 DEG C, and the time of contact is at least 20 seconds, and the first absorption agent and the volume ratio containing lighter hydrocarbons petrochemical complex gas are 1:3.5-6; The condition of described Desorption separation comprises: the time of desorb is 15-30 second, and desorption tower column bottom temperature is 120-160 DEG C, and tower top temperature is 0-50 DEG C.
2. treatment process according to claim 1, wherein, the temperature that described condition contact with the first absorption agent containing lighter hydrocarbons petrochemical complex gas comprises contact is 20-40 DEG C, and the time of contact is 25-50 second, and the first absorption agent and the volume ratio containing lighter hydrocarbons petrochemical complex gas are 1:3.7-5.5.
3. according to the treatment process in claim 1-2 described in any one, wherein, be that the described lighter hydrocarbons petrochemical complex gas that contains is contacted with the first absorption agent is reverse in the first absorption tower by described mode contact with the first absorption agent containing lighter hydrocarbons petrochemical complex gas, and from the first absorption tower recovered overhead first lean gas, described treatment process is also included in before Desorption separation goes out rich ethane gas, is contacted by described first rich absorption liquid with containing lighter hydrocarbons petrochemical complex gas in the first absorption equilibrium tank.
4. treatment process according to claim 3, wherein, described first rich absorption liquid is 20-50 DEG C with the temperature contacted in the first absorption equilibrium tank containing lighter hydrocarbons petrochemical complex gas, and the time is 10-60 second.
5. treatment process according to claim 4, wherein, described first rich absorption liquid is 35-45 DEG C with the temperature contacted in the first absorption equilibrium tank containing lighter hydrocarbons petrochemical complex gas, time 15-40 second.
6. treatment process according to claim 1, wherein, the method also comprises the material after desorb is gone out C3-C4 light ends fractionation through rectifying separation in rectifying tower, obtains stable gasoline.
7. treatment process according to claim 6, wherein, described the condition that material after desorb goes out C3-C4 light ends fractionation through rectifying separation in rectifying tower to be comprised: the temperature at the bottom of rectifying tower is 210-240 DEG C, and tower top temperature is 0-45 DEG C, and the rectifying time is 10-50 second.
8. treatment process according to claim 6, wherein, the method also comprises to be sent in the first absorption tower by gained stable gasoline, as the first absorption agent.
9. treatment process according to claim 3, wherein, described first lean gas that the method also comprises recovery obtains contacts with the second absorption agent is reverse in second absorption tower, first absorbent contents of carrying secretly in described first lean gas is made to be reduced to less than 0.2 % by mole, obtain the second rich absorption liquid and coal mine gas, the coal mine gas obtained and the second rich absorption liquid are reclaimed respectively.
10. treatment process according to claim 9, wherein, describedly to comprise reclaiming described first lean gas that obtains with the second absorption agent reverse condition contacted in second absorption tower, the temperature of contact is 40-60 DEG C, the time of contact is 10-25 second, and the volume ratio of the second absorption agent and the first lean gas is 1:15-30.
11. treatment processs according to claim 9 or 10, wherein, described second absorption agent is diesel oil and/or heavy petrol.
12. according to the treatment process in claim 1-2 and 8 described in any one, and wherein, described first absorption agent is one or more in raw gasline, treated gasoline, petroleum naphtha.
13. according to the treatment process in claim 1-2 described in any one, wherein, with the described total amount containing lighter hydrocarbons petrochemical complex gas for benchmark, the described lighter hydrocarbons petrochemical complex gas that contains contains C2 component 10-50 % by mole, not solidifying component 20-80 % by mole, 10-40 % by mole of C3-C4 component.
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| CN101113365A (en) * | 2006-07-28 | 2008-01-30 | 上海东化环境工程有限公司 | Process for recovering lighter hydrocarbons from refinery dry gas |
| CN101987983A (en) * | 2009-08-03 | 2011-03-23 | 中国石油化工股份有限公司 | Coking rich gas light dydrocarbon recovery method and device thereof |
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