CN107353934A - A kind of method of reduction S Zorb devices octane number loss - Google Patents
A kind of method of reduction S Zorb devices octane number loss Download PDFInfo
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- CN107353934A CN107353934A CN201710620763.XA CN201710620763A CN107353934A CN 107353934 A CN107353934 A CN 107353934A CN 201710620763 A CN201710620763 A CN 201710620763A CN 107353934 A CN107353934 A CN 107353934A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of method of reduction S Zorb devices octane number loss, comprise the following steps：(1) process operation parameter of Fcc Stabilizer is adjusted, the component of carbon four in S Zorb device raw materials is cut into desulfuration of liquefied gas, gas separation, MTBE synthesis combined units；(2) in combined unit, the desulfurization together with catalytic cracking liquefied gas of the component of carbon four；(3) gas composition after desulfurization is separated, and the component of carbon four isolated enters MTBE devices and carries out etherification reaction；(4) component of unreacted carbon four from MTBE devices enters the middle and upper part of S Zorb device stabilizers, is fractionated after being mixed with gasoline.The present invention can avoid the loss of octane number during gasoline production, reduce hydrogen consumption, alleviate restriction of the S Zorb devices working abilities to whole work flow, realize increasing gasoline yield, cost efficiency.
Description
Technical field
The invention belongs to petroleum refining field, and specifically, S Zorb device octane numbers can be reduced by being related to one kind
The method of loss.
Background technology
With increasingly attention of the countries in the world to environmental protection, super-low sulfur cleaning vapour of the production sulfur content less than 10mg/kg
Oil has become inexorable trend and the requirement of each fuel oil manufacturing enterprise.S Zorb techniques (i.e. adsorbing and desulfurizing catalytic cracking gasoline)
It is one of widely used major technique of production super-low sulfur cleaning domestic and international at present.
Catalytic cracking unit is the most important process units in refinery, is that crude oil process change is the most important of gasoline components
One of manufacturing process, catalytically cracked gasoline have higher sulfur content and octane number, are a kind of wide-cut gasoline component, wherein alkene
Hydrocarbon component content rises and declined with boiling range, sulfur content then rises with boiling range and increases.Vapour pressure of gasoline quality index in the winter time
Under (45~85kPa), the light hydrocarbon component accounting of carbon four therein accounts for half or so, carbon tetraene up to more than 5%, wherein C 4 olefin
Hydrogenation saturated reaction easily occurs during S Zorb device desulphurization reactions for hydrocarbon, while hydrogen consumption is increased, also results in
Octane number reduces.Such as the RON values of n-butene and isobutene be respectively 98.8 and 106.3, and be hydrogenated with the normal butane after saturation and
The RON values of iso-butane are respectively that 93.8 and 99, RON value reduce 5 and 7.3 units respectively, therefore how to be reduced or avoided and urge
Change the saturation during desulfuration purification of the C 4 olefin component in gasoline, it is pungent for the gasoline of reduction super low-sulfur oil production process
The loss of alkane value is significant.
S Zorb devices, will by Special adsorbent under hydrogen environment mainly using components such as catalytically cracked gasolines as raw material
Sulphur in gasoline absorbs, so as to reach the purpose for reducing content of sulfur in gasoline.The feed sulphur content of S Zorb devices typically exists
100-600mg/kg, product sulfur content can reach below 10mg/kg.It is former because absorption desulphurization reaction is carried out in the hydrogen gas atmosphere
Hydrogenation saturated reaction can occur with hydrogen for some olefin component in material, cause the octane number of treated gasoline to reduce, and increased
Journey hydrogen consumption.Research octane number (RON) (RON) loss of current most of S Zorb device of refining gasoline is single at 0.5-1.5
Position, cause lost revenue or influence the production of high-grade gasoline.By taking state V standard motor petrol as an example, No. 92 motor petrol
(RON value >=92) differ 3 units with the RON values of No. 95 motor petrol (RON value >=95), and price differs 360 yuan/ton or so,
The value of equivalent to 1 unit RON value is at 120 yuan/ton, therefore the loss of octane number during reduction deep desulfurization of gasoline is to enterprise
Industry is increased the benefit significant.
For example, Chinese invention patent 201210371143.4 discloses a kind of method for producing super low-sulfur oil, gasoline is former
Material is fractionated into light fraction gasoline and heavy distillat gasoline, and light fraction gasoline enters alkali density unit, and heavy distillat gasoline is in the first hydrogenation
Reactor contacts with catalyst for selectively hydrodesulfurizing to be reacted, and on the basis of the total sulfur in heavy distillat gasoline, removes double distilled
Dividing the sulfide of the heavy % in 90 weight %~95 in gasoline, the reaction effluent of the first hydrogenation reactor enters the second hydrogenation reactor,
Contact and reacted with waste residue oil hydrogenation catalysts, gained, which is refined after light fraction gasoline mixes with hydrogenation heavy distillat gasoline, to be surpassed
Low-sulphur oil cut.The total sulfur content of full distillation gasoline product is less than 10 μ g/g obtained by the technique, and still, its shortcoming is anti-in hydrogen
Hydrogen gas consumption is higher during answering, while RON values are lost close to 1.0 units.
The content of the invention
In view of the shortcomings of the prior art, the purpose of the present invention is to rely on existing work flow, and each production need not filled
Put carry out it is larger it is dynamic change in the case of, will be in catalytic gasoline easily with common process desulfuration purification by optimization control scheme
After the larger other gasoline components of the light end component in part (the predominantly component of carbon four), desulfurization difficulty carry out desulfurization process respectively, then
Fractionation cutting is re-mixed, avoids the loss of octane number of super low-sulfur oil production process, reduces the consumption of subtractive process hydrogen resources,
Alleviate restriction of the S Zorb devices working abilities to full factory's work flow, realize increasing gasoline yield and cost efficiency purpose.
To achieve the above object, technical scheme provided by the invention is：
A kind of method of reduction S Zorb devices octane number loss, comprises the following steps：(1) it is steady to adjust catalytic cracking
Determine the process operation parameter of tower, by the component of carbon four in S Zorb device raw materials be cut into desulfuration of liquefied gas, gas separation,
MTBE synthesizes combined unit；(2) in combined unit, the desulfurization together with catalytic cracking liquefied gas of the component of carbon four；(3) after desulfurization
Gas composition is separated, and the component of carbon four isolated enters MTBE devices and carries out etherification reaction；(4) from MTBE devices not
The component of carbon four of reaction enters the middle and upper part of S Zorb device stabilizers, is fractionated after being mixed with gasoline, adjustment S Zorb dresses
The process operation parameter of stabilizer is put, the saturated vapor pressure of stable gasoline is met gasoline blend component requirement.
Preferably, the column bottom temperature of the Fcc Stabilizer after being adjusted in step (1) is 165 DEG C -178 DEG C, tower top temperature
Spend for 60 DEG C -68 DEG C, tower top pressure 1.0-1.2MPa.
Preferably, step (1) component of carbon four is butane and C 4 olefin.
Preferably, step (2) described sulfur method includes amine absorption method and alkali wash.
Preferably, what the amine absorption method and alkali wash removed is hydrogen sulfide and mercaptan.
Preferably, the 5%-100% of step (4) component of carbon four enters the middle and upper part of S Zorb device stabilizers.
Preferably, the column bottom temperature of the S Zorb device stabilizers after step (4) described adjustment is 115 DEG C -125 DEG C, tower
It is 36 DEG C -45 DEG C to push up temperature, tower top pressure 0.66MPa-0.80Mpa.
Preferably, the saturated vapor pressure of step (4) described stable gasoline is 60kPa-100kPa.
Preferably, the component of unreacted carbon four described in step (4) is gasoline blend component, and its research octane number (RON) is
90-115, sulfur content are less than 10mg/kg.
Equipment therefor of the present invention includes Fcc Stabilizer, desulfuration of liquefied gas, gas separation and MTBE combined units, S
Zorb device reactions system and S Zorb device stabilizers, from the component pipeline of carbon four in combined unit exit draw one across
Line, the cross-line are connected with S Zorb device stabilizers top feeding line.
In the above-mentioned technical solutions, by adjusting catalytic unit absorbing-stabilizing system control program, original is cut into S
The component of most of carbon four of Zorb devices raw material (catalytic gasoline), is cut into catalytic liquefaction gas, and the component of part carbon four is with catalysis
The desulfurization by way of amine absorption and alkali cleaning together of cracking liquefied gas, the liquefied gas component after refining desulfurization separate through gas
After device isolates carbon three, the component of carbon four, the component of carbon four is again through MTBE devices, isobutene therein and methanol reaction generation Gaoxin
The MTBE products (RON values are up to 115) of alkane value, (olefin(e) centent accounts for half or so to other unreacted components of carbon four, and sulfur content is low
In 5mg/kg), S Zorb device stabilizers middle and upper part is partly entered by the technological process newly increased；One other sulfur content compared with
High and larger desulfurization difficulty gasoline component, deliver to after the absorption desulfurization of S Zorb device reactions system, desulfurization enters stabilizer
Middle and lower part.Two bursts of chargings are sufficiently mixed in stabilizer, and production total sulfur content is less than 10mg/kg super low-sulfur oil product,
RON losses are not more than 0.5 unit.
Beneficial effects of the present invention：
(1) existing work flow is relied on, carbon four and other light components pass through amine absorption and alkali cleaning etc. with catalytic liquefaction gas
Mode desulfurization, desulphurization cost is relatively low, olefin saturation does not occur in sweetening process, therefore do not produce loss of octane number；
(2) isobutyl olefinic constituents is advantageous to filling for isobutyl olefinic constituents by MTBE devices and methanol reaction generation MTBE products
Divide and recycle；
(3) charging of S Zorb device reactions system reduces, and reduces the energy resource consumption and adsorbent consumption of reaction system, together
When be advantageous to improve S Zorb devices working ability.
Performance analysis：
Specific benefit calculation is as follows：
(1) octane number loss is reduced：By taking the S Zorb devices of 1,500,000 tons/year of scales as an example, implement this scheme it
Afterwards, the RON value losses of treated gasoline reduce about 0.3 unit, it is contemplated that the method is mainly real during gasoline index in the winter time
(annual November-April) is applied, during which actual processing amount is calculated by 750,000 tons/year of calculating, 1 unit octane number by 120 yuan/ton, often
It is ten thousand yuan of 75*0.3*120=2700 that year, which can increase benefit,；
(2) increasing gasoline yield blend component：The mass fraction of the component of carbon four calculates by 7% in winter S Zorb devices raw material,
MTBE product yields calculate by the 16% of the raw material of carbon four, every year can voluminous ten thousand tons of MTBE products 75*7%*16%=0.84, MTBE
Product calculates with liquefied gas price differential by 1500 yuan/ton, every year can ten thousand yuan of synergy 0.84*1500=1260；
Two total yuan/year of benefit 39,600,000.
Brief description of the drawings
Fig. 1 is the schematic diagram of the equipment therefor of embodiment 1；
Fig. 2 is the schematic diagram of the equipment therefor of comparative example 1.
Label declaration：
1-- Stabilizer In Fccus；2--S Zorb device reaction systems；
3--S Zorb device stabilizers；4-- desulfuration of liquefied gas, gas separation and MTBE combined units；
5-- catalytically cracked gasolines pipeline (i.e. S Zorb devices feeding line)；
6-- catalytic cracking Liquefied petroleum gas pipes；7--S Zorb device stabilizers bottom feeding line；
8--S Zorb device stabilizers top feeding line；9--S Zorb device of refining gasoline products pipelines；
10--S Zorb device stabilizer dry gas pipelines；The component pipeline of 11-- carbon three；
12--MTBE product pipelines；The component pipeline of 13-- carbon four；
The component of 14-- carbon four to S Zorb device stabilizers top feeding line cross-line；
The component of 15-- carbon four is to S Zorb device stabilizer control valves.
Embodiment
The present invention is described in further detail below in conjunction with the accompanying drawings.
Embodiment 1
As shown in figure 1, the bottom gasoline of Fcc Stabilizer 1 is by catalytically cracked gasoline pipeline 5, (i.e. S Zorb devices enter
Expects pipe line) into S Zorb device reactions system 2 carry out absorption desulfurization, the gasoline component after desulphurization reaction is filled by S Zorb
Put stabilizer bottom feeding line 7 and S Zorb device stabilizers top feeding line 8 enters S Zorb devices stabilizer 3 and entered
Row fractionation, dry gas pass through S Zorb devices by the carrying device of S Zorb device stabilizer dry gas pipeline 10, treated gasoline product
Treated gasoline product pipeline 9 delivers to gasoline products tank field.
The top liquefied gas of Fcc Stabilizer 1 enters desulfuration of liquefied gas, gas point by catalytic cracking Liquefied petroleum gas pipe 6
From and MTBE combined units 2 carry out desulfurization, separation and etherification reaction, the component of carbon three separated pass through the component pipeline 11 of carbon three
Carrying device, the MTBE products of generation deliver to MTBE products tank field by MTBE product pipelines 12, and the unreacted component of carbon four is led to
Cross the component pipeline 13 of carbon four and deliver to liquefied gas product tank field.
In above-mentioned catalytic gasoline deep desulfuration technical process, increase on a component of carbon four to S Zorb device stabilizers
The cross-line 14 of portion's feeding line, the component of carbon four is incorporated into S Zorb devices stabilizer 3.
Stabilizer In Fccu operating parameter is optimized and revised, the component of carbon four during S Zorb devices are fed and catalysis
Cracking unit stabilizer tower top liquefied gas is steamed and separated with bottom of towe gasoline together, is removed by way of amine absorption and alkali cleaning
Hydrogen sulfide and mercaptan, subsequently into gas separation and MTBE devices, isobutene therein and methanol reaction generation MTBE products, not
The component of carbon four of reaction enters the top of S Zorb device stabilizers by the cross-line that newly increases, with by absorption desulphurization reaction it
Gasoline afterwards is sufficiently mixed and is fractionated in S Zorb device stabilizer, is operated by adjusting stabilizer, makes bottom of towe gasoline products
Quality meets index request.
Main operating parameters and raw material and product property are as shown in table 1.
Table 1
Embodiment 2
As shown in figure 1, technological process is the same as embodiment 1.
Main operating parameters and raw material and product property are as shown in table 2.
Table 2
Comparative example 1
As shown in Fig. 2 using existing process technology, the bottom gasoline of Fcc Stabilizer 1 passes through catalytically cracked gasoline pipe
Line 5 (i.e. S Zorb devices feeding line) carries out absorption desulfurization into S Zorb device reactions system 2, the vapour after desulphurization reaction
Oil ingredient enters S by S Zorb device stabilizers bottom feeding line 7 and S Zorb device stabilizers top feeding line 8
Zorb devices stabilizer 3 is fractionated, and dry gas passes through the carrying device of S Zorb device stabilizer dry gas pipeline 10, treated gasoline production
Product deliver to gasoline products tank field by S Zorb device of refining gasoline products pipeline 9.
The top liquefied gas of Fcc Stabilizer 1 enters desulfuration of liquefied gas, gas point by catalytic cracking Liquefied petroleum gas pipe 6
From and MTBE combined units 2 carry out desulfurization, separation and etherification reaction, the component of carbon three separated pass through the component pipeline 11 of carbon three
Carrying device, the MTBE products of generation deliver to MTBE products tank field by MTBE product pipelines 12, and the unreacted component of carbon four is led to
Cross the component pipeline 13 of carbon four and deliver to liquefied gas product tank field.
Main operating parameters and raw material and product property are shown in Table 3.
Table 3
The obvious reduction of RON values loss of technology of the present invention is can be seen that from data shown in table 1, table 2 and table 3.
Benefit calculation：
(1) loss of octane number is reduced：Typical condition S Zorb device gasoline products yield is 188t/h, and RON value losses subtract
0.3 unit is lacked, 1 unit octane number is by 120 yuan/ton of calculating, it is contemplated that mainly (annual 11 during gasoline winter index
The April moon-next year) implement the present invention, implement number of days and calculated by 182 days, then can increase benefit every year is：182*24*188*0.3*
Ten thousand yuan of 120=2956.
(2) MTBE products are increased production：MTBE yield adds 1.9t/h, every year can voluminous MTBE products 182*24*1.9=
8299 tons, MTBE products calculate with liquefied gas price differential by 1500 yuan/ton, every year can ten thousand yuan of synergy 8299*1500=1245.
Two total yuan/year of benefit 42,010,000.
Claims (9)
- A kind of 1. method of reduction S Zorb devices octane number loss, it is characterised in that comprise the following steps：(1) adjust The process operation parameter of Fcc Stabilizer, by the component of carbon four in S Zorb device raw materials be cut into desulfuration of liquefied gas, Gas separation, MTBE synthesis combined units；(2) in combined unit, the desulfurization together with catalytic cracking liquefied gas of the component of carbon four； (3) gas composition after desulfurization is separated, and the component of carbon four isolated enters MTBE devices and carries out etherification reaction；(4) come from The component of unreacted carbon four of MTBE devices enters the middle and upper part of S Zorb device stabilizers, is fractionated after being mixed with gasoline, The process operation parameter of S Zorb device stabilizers is adjusted, the saturated vapor pressure of stable gasoline is met that gasoline blend component will Ask.
- A kind of 2. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly the column bottom temperature of the Fcc Stabilizer after being adjusted in (1) is 165 DEG C -178 DEG C, and tower top temperature is 60 DEG C -68 DEG C, tower top Pressure is 1.0-1.2MPa.
- A kind of 3. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly (1) described component of carbon four is butane and C 4 olefin.
- A kind of 4. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly (2) described sulfur method includes amine absorption method and alkali wash.
- A kind of 5. method of reduction S Zorb devices octane number loss according to claim 4, it is characterised in that institute State amine absorption method and alkali wash removing be hydrogen sulfide and mercaptan.
- A kind of 6. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly the 5%-100% of (4) described component of carbon four enters the middle and upper part of S Zorb device stabilizers.
- A kind of 7. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly the column bottom temperature of the S Zorb device stabilizers after (4) described adjustment is 115 DEG C -125 DEG C, and tower top temperature is 36 DEG C -45 DEG C, Tower top pressure is 0.66MPa-0.80Mpa.
- A kind of 8. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly the saturated vapor pressure of (4) described stable gasoline is 60kPa-100kPa.
- A kind of 9. method of reduction S Zorb devices octane number loss according to claim 1, it is characterised in that step Suddenly the component of unreacted carbon four described in (4) is gasoline blend component, and its research octane number (RON) is 90-115, and sulfur content is less than 10mg/kg。
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109207196A (en) * | 2018-10-25 | 2019-01-15 | 中国石油化工股份有限公司 | A kind of FDFCC catalytic cracking modifies the processing flow of secondary raw gasoline |
| US20220380689A1 (en) * | 2019-10-31 | 2022-12-01 | China Petroleum & Chemical Corporation | Method and apparatus for desulfurization and separation of catalytically cracked light product |
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| CN106281442A (en) * | 2015-06-08 | 2017-01-04 | 中国石化工程建设有限公司 | A kind of processing method of catalytically cracked gasoline |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106281442A (en) * | 2015-06-08 | 2017-01-04 | 中国石化工程建设有限公司 | A kind of processing method of catalytically cracked gasoline |
Non-Patent Citations (1)
| Title |
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| 简建超等: "炼油厂国V排放标准汽油生产方案中S Zorb装置的优化", 《石油炼制与化工》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109207196A (en) * | 2018-10-25 | 2019-01-15 | 中国石油化工股份有限公司 | A kind of FDFCC catalytic cracking modifies the processing flow of secondary raw gasoline |
| US20220380689A1 (en) * | 2019-10-31 | 2022-12-01 | China Petroleum & Chemical Corporation | Method and apparatus for desulfurization and separation of catalytically cracked light product |
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