CN205011709U - DCC schizolysis light oil system of processing - Google Patents
DCC schizolysis light oil system of processing Download PDFInfo
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- CN205011709U CN205011709U CN201520575925.9U CN201520575925U CN205011709U CN 205011709 U CN205011709 U CN 205011709U CN 201520575925 U CN201520575925 U CN 201520575925U CN 205011709 U CN205011709 U CN 205011709U
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Abstract
The utility model belongs to the technical field of petrochemical, concretely relates to DCC schizolysis light oil system of processing, improved design have a three bed reactor, mainly are the schizolysis light oil with the production of DCC device, behind degree of depth hydrogenation, upgrading, producing country IV, compromise V diesel oil in the state and mediate the component. This process route is refine - the hydrodewaxing device in line with as far as possible sharp old 400, 000 tons of / year former diesel oil hydrogenation to can satisfy the principle of schizolysis light oil oil hydrogenation technology demand, through reforming transform, processing catalytic cracking (DCC) makes the schizolysis light oil product of ethylene plant by -product, and this system not only can show sulphur and the nitrogen that reduces wherein, can also improve schizolysis light oil cetane number, and it can consonant diesel oil component to obtain. The technology of this system is first set internal DCC schizolysis light oil hydrogenation technology, and the successful operation of this technology can not only provide the reliable assurance, the popularization and the application of the DCC technology of having made greater efforts to promote in addition for the even running of DCC device.
Description
Technical field
The utility model belongs to technical field of petrochemical industry, is specifically related to a kind of DCC cracking light oil system of processing.
Background technology
Catalytic pyrolysis/catalytic pyrolysis (DCC/CPP) technique is on the basis of fluid catalytic cracking (FCC) technology, is the gaseous olefin of raw material production based on propylene and ethylene, and produces the technology of partially liq product with mink cell focus.The catalyzer adopted due to DCC technique and operational condition are different from traditional FCC technology, and the character of its liquid product also has larger difference.According to the light oil properties of DCC, density (20 DEG C) is 0.9532g/cm3, and 95% recovered temperature is 293 DEG C, and sulphur content is 1518g/g, and nitrogen content is 1500g/g, and cetane index is 14.6, and zero pour is-36 DEG C, hydrogen richness 9.14%, carbon content 90.56%.Mass spectrum composition data show, elm can change DCC light oil paraffinicity 10.7%, and naphthene content is 5.1%, and aromaticity content is 84.2%, and state IV, sulphur content is respectively 50 (μ g/g), 10 (μ g/g) in state V motor spirit standard.
DCC cracking light oil is because material density is large, aromaticity content is high, and domestic do not have ripe complete processing temporarily, makes this raw materials market market cheaper, had a strong impact on device economic benefit.
Utility model content
The purpose of this utility model is the needs for tackling the upgrading of national oil quality, for this burst of feature that material density is large, aromaticity content is high, utilize original 400,000 tons/year of diesel oil hydrogenation pour point depression devices, transform a set of DCC cracking light oil system of processing as, carry out hydrofining process, its know-why is when removing the impurity such as sulphur, nitrogen, makes the low cetane value hydrocarbons hydrogenation open loop not chain ruptures such as polycyclic aromatic hydrocarbons, thus reaches and increase substantially diesel cetane-number.
For this reason, the utility model provides a kind of DCC cracking light oil system of processing, comprise automatic backwashing filter, stock oil water distributing can, stock oil surge tank, high pressure feedstock oil pump, interchanger, hydrogenator, gas-liquid separator and stripping tower, described backwash filter, stock oil water distributing can, stock oil surge tank, high pressure feedstock oil pump connects in turn, high pressure feedstock oil pump outlet connects interchanger C successively by pipeline, interchanger A, the tower top of hydrogenator is communicated to after process furnace, the tower bottom outlet of hydrogenator connects interchanger A successively by pipeline, interchanger B, high-pressure separator is communicated to after air cooler,
The pneumatic outlet of described high-pressure separator is communicated to gas-liquid separator, the liquid exit of high-pressure separator is communicated to light pressure separator, the pneumatic outlet of gas-liquid separator is communicated to hydrogenator, after interchanger D, interchanger B, be communicated to stripping tower again behind the liquid exit of gas-liquid separator and the liquid exit interflow of light pressure separator, described high-pressure separator and the sewage outlet of light pressure separator are communicated to waste disposal plant;
The tower top outlet of described stripping tower connects air cooler and return tank successively, and the gaseous phase outlet of return tank is communicated to gas concentration unit, and the aqueous phase outlet of return tank is to water softener tank, and the outlet of return tank oil phase connects the tower tray of petrol storage tanks and stripping tower;
Diesel oil storage tank is communicated to after the tower bottom outlet of described stripping tower connects diesel oil pump, interchanger D, product air cooler successively by pipeline.
DCC cracking light oil system of processing also comprises new hydrogen dosage unit, and this new hydrogen dosage unit comprises new hydrogen charging opening, and new hydrogen charging opening connects compressor, and the outlet of compressor is to the outlet external transport pipeline of high pressure stock oil.
The external transport pipeline of the outlet of described compressor also collaborates with the external transport pipeline of the pneumatic outlet of gas-liquid separator to be communicated to high pressure feedstock oil pump outlet external transport pipeline.
The liquid exit of described gas-liquid separator is also communicated with stock oil water distributing can with the pipeline behind the liquid exit interflow of light pressure separator.
Described hydrogenator divides three beds, is equipped with catalyzer in upper bed layer: protective material FZC-106, protective material FZC-105 and finishing agent FHUDS-6, and three's mass ratio is 0.97:1:9.45; Catalyzer is equipped with: FHUDS-6 finishing agent in middle bed; Catalyzer is equipped with: transformation of the way agent FC-16 and finishing agent FHUDS-6, both mass ratios are 21.50:4.67 in lower bed layer.
The pneumatic outlet of described gas-liquid separator is all communicated with the upper, middle and lower of hydrogenator three layers.
The beneficial effects of the utility model: the DCC cracking light oil system of processing that the utility model provides, its technique not only significantly can reduce sulphur wherein and nitrogen, can also improve cracking light oil cetane value, obtain the diesel component that can be in harmonious proportion.This technique is domestic first cover DCC cracking light oil hydrogenation technique, and the successful operation of this technique, the smooth running not being only DCC device provides Reliable guarantee, and the promotion and application of DCC technique of having made greater efforts to promote.
Accompanying drawing explanation
Below with reference to accompanying drawing, the utility model is described in further details.
Fig. 1 is system flow schematic diagram of the present utility model.
Description of reference numerals: 1, automatic backwashing filter; 2, stock oil water distributing can; 3, stock oil surge tank; 4, high pressure feedstock oil pump; 5, hydrogenator; 6, gas-liquid separator; 7, stripping tower; 8, interchanger C; 9, interchanger A; 10, process furnace; 11, interchanger B; 12, air cooler; 13, high-pressure separator; 14, light pressure separator; 15, interchanger D; 16, air cooler; 17, return tank; 18, diesel oil pump; 19, air cooler; 20, new hydrogen charging opening; 21, compressor.
Embodiment
Embodiment 1:
The present embodiment provides a kind of DCC cracking light oil system of processing, as shown in Figure 1, comprise automatic backwashing filter 1, stock oil water distributing can 2, stock oil surge tank 3, high pressure feedstock oil pump 4, interchanger, hydrogenator 5, gas-liquid separator 6 and stripping tower 7, described backwash filter 1, stock oil water distributing can 2, stock oil surge tank 3, high pressure feedstock oil pump 4 connects in turn, the outlet of high pressure feedstock oil pump 4 connects interchanger C8 successively by pipeline, interchanger A9, the tower top of hydrogenator 5 is communicated to after process furnace 10, the tower bottom outlet of hydrogenator 5 connects interchanger A9 successively by pipeline, interchanger B11, high-pressure separator 13 is communicated to after air cooler 12.
The pneumatic outlet of high-pressure separator 13 is communicated to gas-liquid separator 6, the liquid exit of high-pressure separator 13 is communicated to light pressure separator 14, the pneumatic outlet of gas-liquid separator 6 is communicated to hydrogenator 5, after interchanger D15, interchanger B11, be communicated to stripping tower 7 again behind the liquid exit of gas-liquid separator 6 and the liquid exit interflow of light pressure separator 14, described high-pressure separator 13 and the sewage outlet of light pressure separator 14 are communicated to waste disposal plant.
The tower top outlet of stripping tower 7 connects air cooler 16 and return tank 17 successively, the gaseous phase outlet of return tank 17 is communicated to gas concentration unit, the aqueous phase outlet of return tank 17 is to water softener tank, and the outlet of return tank 17 oil phase connects the tower tray of petrol storage tanks and stripping tower 7.
Diesel oil storage tank is communicated to after the tower bottom outlet of stripping tower 7 connects diesel oil pump 18, interchanger D15, product air cooler 19 successively by pipeline.
DCC cracking light oil system of processing also comprises new hydrogen dosage unit, and this new hydrogen dosage unit comprises new hydrogen charging opening 20, and new hydrogen charging opening 20 connects compressor 21, and the outlet of compressor 21 is to the outlet external transport pipeline of high pressure raw oil pump 4.
The external transport pipeline of the outlet of compressor 21 also collaborates with the external transport pipeline of the pneumatic outlet of gas-liquid separator 6 the outlet external transport pipeline being communicated to high pressure feedstock oil pump 4.
The liquid exit of gas-liquid separator 6 is also communicated with stock oil water distributing can 2 with the pipeline behind the liquid exit interflow of light pressure separator 14.
Hydrogenator 5 points of three beds, be equipped with catalyzer in upper bed layer: protective material FZC-106, protective material FZC-105 and finishing agent FHUDS-6, three's mass ratio is 0.97:1:9.45; Catalyzer is equipped with: FHUDS-6 finishing agent in middle bed; Catalyzer is equipped with: transformation of the way agent FC-16 and finishing agent FHUDS-6, both mass ratios are 21.50:4.67 in lower bed layer.
The pneumatic outlet of gas-liquid separator 6 is all communicated with the upper, middle and lower of hydrogenator 5 three layers.
The technological process of this DCC cracking light oil system of processing of the present embodiment is as follows:
Step one: the DCC cracking light oil come from tank field cuts out free-water, then incoming stock oily surge tank 3 through automatic backwashing filter 1 and stock oil water distributing can 2 elimination solid impurity successively, then boosts to 6.8 ~ 7.8MPa through high pressure feedstock oil pump 4.
Step 2: by the new hydrogen of new hydrogen charging opening 20, after make-up hydrogen compressor 21 is forced into 6.8 ~ 7.8MPa, stock oil mixing after the boosting obtained with step one again, the blending ratio of new hydrogen and stock oil is: 1 ton of raw material oil consumption hydrogen 0.016 ton, obtain mixed hydrogen stock oil, mixed hydrogen stock oil, successively through interchanger C8 heat exchange to 150 ~ 180 DEG C with interchanger A9 heat exchange to 250 ~ 280 DEG C, enters reaction heating furnace 10 and is warming up to 290 ~ 320 °, then enter hydrogenator 5.
Step 3: in hydrogenator 5, mixed hydrogen stock oil, under catalyst action, carries out hydrogenating desulfurization, denitrogenation, deoxidation, alkene and aromatic hydrogenation saturated reaction.Hydrogenator 5 points of upper, middle and lowers three beds, catalyzer in hydrogenator 5 is: Hydrobon catalyst FHUDS-6, catalyst for hydro-upgrading FC-18, protective material FZC-105 and protective material FZC-106, catalyzer in upper bed layer is protective material FZC-106, protective material FZC-105 and finishing agent FHUDS-6, and three's mass ratio is 0.97:1:9.45; Catalyzer in middle bed is FHUDS-6 finishing agent; Catalyzer in lower bed layer is transformation of the way agent FC-18 and finishing agent FHUDS-6, and both mass ratios are 23.50:4.67.
Reaction product flows out bottom hydrogenator 5, successively through interchanger A9 heat exchange to 210 ~ 250 DEG C, through interchanger B11 heat exchange to 170 ~ 210 DEG C, interchanger C8 tri-heat exchange to 90 ~ 130 DEG C, enter high-pressure air cooler 12, reaction product is after high-pressure air cooler 12 is cooled to 45 DEG C, enter high-pressure separator 13, for preventing separating out ammonia salt in reaction product process of cooling and blocking pipe and equipment, by high pressure water-injection pump, de-mineralized water is injected high-pressure air cooler inlet line, dissolve scrubbing ammonia salt.
Step 4: in high-pressure separator 13, carries out gas, oil, water three phase separation,
The fluid that high-pressure separator 13 is separated enters light pressure separator 14 and is again separated, and the sour water that high-pressure separator 13 is separated with light pressure separator 14 is delivered to waste disposal plant and processed, and such as directly passes into sulfur-containing sewage stripping device and processes;
The gas phase that high-pressure separator 13 is separated is flowed out by high-pressure separator 13 top and enters gas-liquid separator 6 separatory, the liquid phase that gas-liquid separator 6 is separated is gone out by tank underflow, the gas phase that gas-liquid separator 6 is separated then is flowed out by tank deck, 7.0 ~ 7.5MPa is boosted to through compressor, be divided into two-way, wherein a road enters hydrogenator 5 as quenching hydrogen and controls bed temperature, this hydrogenator 5 is divided into, in, lower three beds, quenching hydrogen is divided into three tunnels and enters the upper of hydrogenator respectively, in, lower three beds, three bed temperature rise ratios are made to remain 20 DEG C respectively, 28 DEG C and 55 DEG C, namely at the production initial stage, after process furnace 10 is heated to 290 ~ 320 °, enter hydrogenator 5, first 55 DEG C are heated up at lower bed layer, then enter middle bed and heat up 28 DEG C, finally enter upper strata bed, heat up 20 DEG C.
The gas phase of compressor boosting is except as except quenching hydrogen, and remaining is mixed into the new hydrogen from make-up hydrogen compressor 21 and mixes hydrogen, and the stock oil after the boosting obtained with step one together mixes, and obtains mixed hydrogen stock oil.
Two portions are divided into after the liquid-phase mixing that the fluid obtained after light pressure separator 14 is separated and gas-liquid separator 6 underflow go out, a part reenters the raw material surge tank 2 in step one, another part successively through interchanger D15 heat exchange to 185 ± 10 DEG C, behind interchanger B11 heat exchange to 225 ± 10 DEG C, enter stripping tower 7, this two-part ratio is 1:1.
Step 5: the oil gas in stripping tower 7 is flowed out by tower top, enter after air cooler 16 is cooled to 40 DEG C, then enter return tank 17 and carry out gas, oil, water three phase separation, the isolated gas phase of return tank 17 delivers to the recycling of gas concentration unit products for further, here gas is the equal of a kind of byproduct, can decide specifically to process direction according to real needs; The isolated aqueous phase of return tank 17 delivers to water softener tank; The isolated raw gasline of return tank 17 is extracted out by raw gasline pump, a part is got on stripping tower head tower dish as backflow, it is stand-by that another part raw gasline is recycled to petrol storage tanks, on the basis ensureing backflow, remaining raw gasline is collected stand-by as a kind of byproduct, here, the ratio of the raw gasline that the isolated raw gasline of return tank 17 is got on stripping tower head tower dish and recovery is stand-by is 20:1.
Refined diesel oil out at the bottom of the tower of stripping tower 7 is forced into through diesel oil pump 18 that to enter interchanger D15(tube side material after 0.8MPa be oil at the bottom of tower, shell side material is low point of oil, during normal operation, by-pass walked by shell side material), behind interchanger D15 heat exchange to 185 ± 10 DEG C, be cooled to 50 DEG C through diesel product air cooler 19, then store in Diesel oil storage tank as product-collecting.
Finally, this technical process realizes DCC cracking light oil machining process, obtains raw gasline and diesel oil, and the multiple byproduct produced in technological process, in can again being utilized Alternative to circulate, significantly reduces production cost.This DCC cracking light oil complete processing not only significantly can reduce sulphur wherein and nitrogen, can also improve cracking light oil cetane value, obtain the diesel component that can be in harmonious proportion.This technique is domestic first cover DCC cracking light oil hydrogenation technique, and the successful operation of this technique, can not only provide Reliable guarantee for the smooth running of DCC device, and the promotion and application of DCC technique of having made greater efforts to promote.
Embodiment 2:
Be described below in conjunction with concrete implementation data.
First, the DCC cracking light oil come from tank field cuts out free-water, then incoming stock oily surge tank 3 through automatic backwashing filter 1 and stock oil water distributing can 2 elimination solid impurity successively, then boosts to 7.3MPa through high pressure feedstock oil pump 4; On the other hand, by the new hydrogen of new hydrogen charging opening 20, after make-up hydrogen compressor 21 is forced into 7.3MPa, stock oil mixing after the boosting obtained with step one again, the blending ratio of new hydrogen and stock oil is: 1 ton of raw material oil consumption hydrogen 0.016 ton, obtains mixed hydrogen stock oil, and mixed hydrogen stock oil is successively through interchanger C8 heat exchange to 165 DEG C and interchanger A9 heat exchange to 265 DEG C, enter reaction heating furnace 10 and be warming up to 312 °, then enter hydrogenator 5.
In hydrogenator 5, mixed hydrogen stock oil, under catalyst action, carries out hydrogenating desulfurization, denitrogenation, deoxidation, alkene and aromatic hydrogenation saturated reaction.In the present embodiment; hydrogenator 5 points of upper, middle and lowers three beds, the catalyzer in hydrogenator 5 is: upper bed layer (FZC-106 protective material 0.97 ton, FZC-105 protective material 1 ton, FHUDS-6 finishing agent 9.45 tons), middle bed (FHUDS-6 finishing agent 19.55 tons), lower bed layer (FC-18 changes a social system agent 23.50 tons, FHUDS-6 finishing agent 4.67 tons).
Reaction product flows out bottom hydrogenator 5, successively through interchanger A9 heat exchange to 230 DEG C, through interchanger B11 heat exchange to 190 DEG C, interchanger C8 tri-heat exchange to 110 DEG C, enter high-pressure air cooler 12, reaction product is after high-pressure air cooler 12 is cooled to 45 DEG C, enter high-pressure separator 13, for preventing from separating out in reaction product process of cooling ammonia salt and blocking pipe and equipment, by high pressure water-injection pump, de-mineralized water being injected high-pressure air cooler inlet line, dissolving scrubbing ammonia salt.
In high-pressure separator 13, carry out gas, oil, water three phase separation,
The fluid that high-pressure separator 13 is separated enters light pressure separator 14 and is again separated, and the sour water that high-pressure separator 13 is separated with light pressure separator 14 delivers to the outer sulfur-containing sewage stripping device process of device;
The gas phase that high-pressure separator 13 is separated is flowed out by high-pressure separator 13 top and enters gas-liquid separator 6 separatory, the liquid phase that gas-liquid separator 6 is separated is gone out by tank underflow, the gas phase that gas-liquid separator 6 is separated then is flowed out by tank deck, 7.3MPa is boosted to through compressor, be divided into two-way, wherein a road enters hydrogenator 5 as quenching hydrogen and controls bed temperature, this hydrogenator 5 is divided into, in, lower three beds, quenching hydrogen is divided into three tunnels and enters the upper of hydrogenator 5 respectively, in, lower three beds, three bed temperature rise ratios are made to remain 20 DEG C respectively, 28 DEG C and 55 DEG C, namely at the production initial stage, after process furnace is heated to 312 DEG C, enter hydrogenator 5, first 55 DEG C are heated up at lower bed layer, temperature rises to 367 DEG C, then enter middle bed and heat up 28 DEG C, owing to having thermal losses in reaction process, therefore the actual temperature entering the reactant of middle bed is approximately 349 DEG C, heat up 28 DEG C, with partial heat loss, temperature rises to 353 DEG C, finally enter upper strata bed, heat up 20 DEG C, outlet temperature is 373 DEG C.
The gas phase of compressor boosting is except as except quenching hydrogen, and remaining is mixed into the new hydrogen from make-up hydrogen compressor 21 and mixes hydrogen, and the stock oil after the boosting obtained with step one together mixes, and obtains mixed hydrogen stock oil.
Two portions are divided into after the liquid-phase mixing that the fluid obtained after light pressure separator 14 is separated and gas-liquid separator underflow go out, a part reenters the raw material surge tank 3 in step one, another part successively through interchanger D15 heat exchange to 185 DEG C, after interchanger B11 heat exchange to 225 DEG C, enter stripping tower 7, this two-part ratio is 1:1.
Oil gas in stripping tower 7 is flowed out by tower top, enter after air cooler 16 is cooled to 40 DEG C, then enter return tank 17 and carry out gas, oil, water three phase separation, the isolated gas phase of return tank 17 delivers to the recycling of gas concentration unit products for further, here gas is the equal of a kind of byproduct, can decide specifically to process direction according to real needs; The isolated aqueous phase of return tank 17 delivers to water softener tank; The isolated raw gasline of return tank 17 is extracted out by raw gasline pump, a part is got on stripping tower 7 head tower dish as backflow, it is stand-by that another part raw gasline is recycled to petrol storage tanks, on the basis ensureing backflow, remaining raw gasline is collected stand-by as a kind of byproduct, here, the ratio of the raw gasline that the isolated raw gasline of return tank 17 is got on stripping tower head tower dish and recovery is stand-by is 20:1.
Refined diesel oil out at the bottom of the tower of stripping tower 7 is forced into through diesel oil pump 18 that to enter interchanger D15(tube side material after 0.8MPa be oil at the bottom of tower, shell side material is low point of oil, during normal operation, by-pass walked by shell side material), after interchanger D15 heat exchange to 185 DEG C, be cooled to 50 DEG C through diesel product air cooler 19, then get up as product-collecting.
More than exemplifying is only illustrate of the present invention, does not form the restriction to protection scope of the present invention, everyly all belongs within protection scope of the present invention with the same or analogous design of the present invention.The parts that the present embodiment does not describe in detail and structure belong to the well-known components of the industry and common structure or conventional means, do not describe one by one here.
Claims (6)
1. a DCC cracking light oil system of processing, comprise automatic backwashing filter (1), stock oil water distributing can (2), stock oil surge tank (3), high pressure feedstock oil pump (4), interchanger, hydrogenator (5), gas-liquid separator (6) and stripping tower (7), it is characterized in that: described backwash filter (1), stock oil water distributing can (2), stock oil surge tank (3), high pressure feedstock oil pump (4) connects in turn, the outlet of high pressure feedstock oil pump (4) connects interchanger C(8 successively by pipeline), interchanger A(9), the tower top of hydrogenator (5) is communicated to after process furnace (10), the tower bottom outlet of hydrogenator (5) connects interchanger A(9 successively by pipeline), interchanger B(11), high-pressure separator (13) is communicated to after air cooler (12),
The pneumatic outlet of described high-pressure separator (13) is communicated to gas-liquid separator (6), the liquid exit of high-pressure separator (13) is communicated to light pressure separator (14), the pneumatic outlet of gas-liquid separator (6) is communicated to hydrogenator (5), again through interchanger D(15 behind the liquid exit interflow of the liquid exit of gas-liquid separator (6) and light pressure separator (14)), interchanger B(11) after be communicated to stripping tower (7), described high-pressure separator (13) and the sewage outlet of light pressure separator (14) are communicated to waste disposal plant;
The tower top outlet of described stripping tower (7) connects air cooler (16) and return tank (17) successively, the gaseous phase outlet of return tank (17) is communicated to gas concentration unit, the aqueous phase outlet of return tank (17) is to water softener tank, and the outlet of return tank (17) oil phase connects the tower tray of petrol storage tanks and stripping tower (7);
The tower bottom outlet of described stripping tower (7) connects diesel oil pump (18), interchanger D(15 successively by pipeline), product air cooler is communicated to Diesel oil storage tank after (19).
2. DCC cracking light oil system of processing as claimed in claim 1, it is characterized in that: DCC cracking light oil system of processing also comprises new hydrogen dosage unit, this new hydrogen dosage unit comprises new hydrogen charging opening (20), new hydrogen charging opening (20) connects compressor (21), and the outlet of compressor (21) is to the outlet external transport pipeline of high pressure raw oil pump (4).
3. DCC cracking light oil system of processing as claimed in claim 2, is characterized in that: the external transport pipeline of the outlet of described compressor (21) also collaborates to be communicated to the outlet external transport pipeline of high pressure feedstock oil pump (4) with the external transport pipeline of the pneumatic outlet of gas-liquid separator (6).
4. the DCC cracking light oil system of processing as described in claim 1 or 2 or 3, is characterized in that: the liquid exit of described gas-liquid separator (6) is also communicated with stock oil water distributing can (2) with the pipeline behind the liquid exit interflow of light pressure separator (14).
5. DCC cracking light oil system of processing as claimed in claim 1, is characterized in that: described hydrogenator (5) point three beds, are equipped with catalyzer in upper bed layer: protective material FZC-106, protective material FZC-105 and finishing agent FHUDS-6; Catalyzer is equipped with: FHUDS-6 finishing agent in middle bed; Catalyzer is equipped with: transformation of the way agent FC-16 and finishing agent FHUDS-6 in lower bed layer.
6. DCC cracking light oil system of processing as claimed in claim 5, is characterized in that: the pneumatic outlet of described gas-liquid separator (6) is all communicated with the upper, middle and lower three layers of hydrogenator (5).
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| CN201520575925.9U CN205011709U (en) | 2015-08-04 | 2015-08-04 | DCC schizolysis light oil system of processing |
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| CN201520575925.9U CN205011709U (en) | 2015-08-04 | 2015-08-04 | DCC schizolysis light oil system of processing |
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| CN201520575925.9U Expired - Fee Related CN205011709U (en) | 2015-08-04 | 2015-08-04 | DCC schizolysis light oil system of processing |
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