CN1765455A - Separation method of hydrocarbon reaction oil gas - Google Patents
Separation method of hydrocarbon reaction oil gas Download PDFInfo
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- CN1765455A CN1765455A CN 200410086224 CN200410086224A CN1765455A CN 1765455 A CN1765455 A CN 1765455A CN 200410086224 CN200410086224 CN 200410086224 CN 200410086224 A CN200410086224 A CN 200410086224A CN 1765455 A CN1765455 A CN 1765455A
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Abstract
Disclosed a separation method of hydrocarbon reaction oil-gas transfers the catalytic cracking reaction oil-gas with C2-C4 hydrocarbon via the bottom into the preliminary fractional tower comprising a tower kettle, a cooling washing area, and a heat transfer fractional area, to be contacted with the catalytic cracking heavy raw material adverse current which is filled from the top of tower. Then the catalyst grains in the reaction oil-gas are removed in the tower kettle and the cooling washing area while the temperature is reduced too; the temperature of reaction oil-gas is reduced more and the heavy components are condensed to be fed into heavy raw material, in the heat transfer fractional area; the temperature reduced reaction oil-gas via the top of preliminary fractional tower is transferred to the following separation system; the temperature of heavy raw material is increased in the process of flowing downwards along the heat transfer fractional area, to be extracted in this process as the raw oil to be fed into catalytic cracking reactor. The invention can realize the simple and effective separation on the high temperature and high gas concentration reaction oil-gas with the catalyst grains.
Description
Technical field
The present invention relates to the separation method of catalytic cracking reaction oil gas, specifically, is the separation method of the catalytic cracking reaction oil gas of a kind of C2 of being rich in, C3, C4 hydro carbons.
Background technology
Fluid catalytic cracking is one of important process of oil secondary operations, and it adopts acidic solid catalyst to contact, react with petroleum hydrocarbon in the mode of fluidisation attitude, and the heavy crude hydro carbons is converted into oils and low-carbon (LC) hydro carbons such as petrol and diesel oil.Along with the shortage of lightweight material oil, utilize heavy charge to produce low-carbon alkene at present, become a kind of trend of development by the method for catalytic cracking.
CN1069016A discloses a kind of catalysis conversion method that utilizes the heavy crude hydro carbons to produce low-carbon alkene, select solid acid catalyst for use, at reaction temperature 650-900 ℃, oil ratio is under the condition of 5-35, and the productive rate of ethene+propylene+butylene can reach 30-40m%.CN1083092A, CN1218786A, CN1403540A disclose the method for similarly producing ethene and propylene.
Its significant process characteristic of method that adopts fluid catalytic cracking to produce low-carbon alkene is: the reaction temperature height, oil ratio is big, the reaction time is short etc.Because the reaction temperature of preparing low-carbon olefin by catalytically cracking is 600-900 ℃, for avoid the high-temperature oil gas green coke that condenses in oil and gas pipes, the reaction oil gas that comes out from reactor will carry out refrigerated separation.At present, mainly adopting direct cooling method or indirect cooling method aspect the cooling of high-temperature oil gas, adopting plate distillation column aspect the separation of hydro carbons more.
CN1100851C discloses a kind of quench tower and quick cooling method of hydro carbons fluidisation catalytic conversion reaction product.Its quench tower middle part is provided with baffle plate, is divided into chilling heat transfer zone and catalyst detergent district.Cat head is the gas phase separation district, is provided with the liquid level control zone at the bottom of tower, is provided with thermal response logistics feed pipe and dust-laden quench liquid outlet.The import of quench liquid is located at heat transfer zone and catalyst dust scrubbing section top.Its method is that reaction oil gas is entered the quench tower bottom, and reactant flows to be gone up by chilling heat transfer zone and catalyst detergent district, and with downward quench liquid counter current contacting heat exchange, the minor amount of catalyst particles that has in the reactant is also taken away by quench liquid simultaneously.Oil gas after the cooling goes out quench tower by the gas phase separation district.Reaction oil gas to about 300-400 ℃, carries out later separation from 670-730 ℃ greenhouse cooling then in quench tower.
" ethene engineering " provided the separation process of preparing ethylene by steam cracking.Pyrolysis furnace outlet Pintsch process gas in the distillate cracker, in waste heat boiler (indirect heat exchanger), carry out indirect heat exchange with water and steam, to reclaim the heat of high-temperature oil gas, high-temperature oil gas (typical temperature is about 780-900 ℃) cools to about 450-600 ℃ according to the difference of cracking stock.The major advantage that adopts indirect heat exchange be can by with the heat exchange of water, the generation high steam effectively utilizes elevated temperature heat.When if cracking stock is heavier, need corresponding raising oil gas heat exchange outlet temperature, prevent that temperature is lower than oil gas dew point generation coking, influences the cycle of operation of heat exchanger.
For typical catalytic cracking FCC technology piece-rate system, reaction oil gas enters the fractionating column bottom, is divided into different intermediate products at fractionating column, and cat head is raw gasoline and rich gas, and side line has diesel oil and freshening wet goods.The gasoline of cat head further separates through absorbing to stablize with rich gas again, behind diesel oil process stripping, the cooling heat transferring, goes out device as finished product.
US6576805 discloses a kind of petroleum hydrocarbon separation method that is rich in low-carbon alkene.Oil gas at first enters main fractionating tower and is separated into heavy-cycle oil, diesel oil distillate behind the catalytic cracking reaction, and cat head is gasoline fraction and gas (moisture), and moisture is through multi-stage compression and cooling, with C3 and C3
-With C3
+Separate C3
+Through isolating C4 and gasoline fraction behind stripper and the stabilizer.C3 and C3
-Cut is through refining, dry, enters follow-up cryogenic separation system, and through domethanizing column, dethanizer and depropanizing tower, ethene separates with propylene the most at last.
In the separation of handling dust-laden oil gas, generally take special structure to prevent the deposition of high-temperature oil gas coking and dust in the bottom of fractionating column, at the general herringbone baffle plate that adopts in the main fractionating tower bottom of catalytic cracking, corresponding baffle arrangement has also been adopted in the disclosed quench tower of CN1100851C bottom.It is big that the herringbone baffle arrangement has circulation, and catalyst dust is rinsed easily, be difficult for characteristics such as deposition, but during as a heat transfer, mass transfer separating member, a significant disadvantages is to have the easy short circuit of oil gas, and the gas-liquid two-phase contacting efficiency is low.
Aspect raising gas-liquid two-phase contacting efficiency, existing document has been announced many different filling-material structures and column plate pattern with patent, such as adopting structured packing, distillation tray etc.CN1116925C has announced a kind of structured packing, and the ripple bearing of trend on the corrugated plating is opposite with fluid flow direction above it, and each layer filler is made of the polylith corrugated plating, between two adjacent corrugated platings certain included angle is arranged.Having a device that reduces the pressure drop that continuous phase produced from a packing element when next packing element flows on the interface of adjacent packing element.The major advantage of this filler has guaranteed good gas-liquid two-phase contacting efficiency for the conversion by the filler angle.
CN1358565A has announced the filler of using in a kind of mass transfer column, and packing section has a plurality of vertical orientated and have the packing sheet that the oblique angle intersects, and it is high to form a section.Each section be high to have a bottom section, a body regions and a top area.Bottom section has the given shape that is different from the body regions geometry, and top area also is different from the body geometry.Realize and change the various usefulness of tower by the geometry that changes different sections.
CN2183817Y has announced a kind of compounded mix form, is made up of inclined type ripple packing and horizontal ripple packing, and two-layer inclined type ripple packing and two-layer horizontal ripple packing are formed a filler unit.Adopt this structure that liquid re-distributor can be set, and have that flux is big, pressure drop is low and characteristics such as efficient height.Because the catalytic pyrolysis gas production is big, reaction oil gas temperature height, be subjected to the restriction of interior gas phase linear speed of tower and thermic load, the separation process of conventional FCC main fractionating tower has been difficult to adapt to this separation requirement.In addition, owing to contain solid catalyst particle in the heaviness of cracking stock and the cracking gas, therefore the separation process of traditional preparing ethylene by steam cracking is not suitable for the preparing low-carbon olefin by catalytically cracking technical process yet.And for the ordinary construction filler, in the petroleum hydrocarbon that contains catalyst granules separated, catalyst particles stopped up the filler duct easily, also causes the coking of high-temperature oil gas easily.
Summary of the invention
The heat exchange separation method that the purpose of this invention is to provide a kind of hydrocarbon reaction oil gas makes the reaction oil gas of high temperature, high gas content and entrained catalyst particles effectively be cooled off and separates.
Method provided by the invention is as follows: the catalytic cracking reaction oil gas that is rich in the C2-C4 hydro carbons enters cold the changing that comprises tower still, cooling scrubbing section and heat exchange fractionation zone by the bottom and presorts in the tower, with the catalytic pyrolysis heavy charge counter current contacting of being injected by this top of tower; The catalyst granules that removes in the reaction oil gas to be carried secretly at tower still and cooling scrubbing section; Progressively reduce the temperature of reaction oil gas and make under the heavy ends condensation in the reaction oil gas at the heat exchange fractionation zone and enter in the heavy charge; Reaction oil gas after the cooling is delivered to subsequent separation system through this cold top of presorting tower of changing; The heavy charge temperature that in the process that flows downward along the heat exchange fractionation zone, progressively raises, and behind the heat exchange fractionation zone of flowing through, be drawn out of, deliver to catalytic cracking reaction device or hydrotreating reactor as feedstock oil.
Compared with prior art, beneficial effect of the present invention is mainly reflected in following aspect:
1. cooling scrubbing section of the present invention is provided with multilayer baffle-type inner member, reaction oil gas and heavy charge separately flow direction when flowing through each layer baffle plate is changed, prolonged the oil gas time of staying, improved heat transfer, the mass-transfer efficiency of gas-liquid two-phase, heavy oil component (boiling range is greater than the 530 ℃) condensation in the assurance reaction oil gas is in heavy charge.In addition, the inner member structure of high voidage guaranteed cold change presort tower can normal running under high gas phase load.
2. heavy oil feedstock and product are presorted direct heat transfer in the tower in cooling, can make reaction oil gas cooling rapidly in a short period of time on the one hand, have meanwhile heated heavy oil feedstock, have saved a large amount of heat transmission equipments; Unreacted on the other hand active principle (diesel oil distillate and boiling range less than 530 ℃ component) presorts in cooling that condensation becomes liquid phase in the tower, has played fractionating effect.The heavy charge that the little amount of catalyst dust of carrying secretly in the oil gas is in addition flowed downward washs and draws at the bottom of tower.
3. the heavy oil feedstock of catalytic pyrolysis needs to improve its character by the hydrogenation preliminary treatment sometimes.The present invention presorts in the tower and the direct contact heat-exchanging of catalytic pyrolysis product by making heavy oil feedstock in cooling, can be heated the required temperature of hydrogenation reaction, needn't establish raw materials furnace and heating in addition, the feeding temperature of hydrogenation reactor can be extracted the position adjustments of mouth out by changing side line, simplified flow process, Btu utilization fully, rationally.
4. the heavy oil component in the catalytic cracking reaction oil gas product can be partly or entirely directly spray into regenerator as combustion oil after presorting tower to enter the tower still and uses through cold changing, to replenish the required heat of catalytic cracking reaction.According to the demand of the heat balance of regenerator, unnecessary slurry oil can be by regulating the output of side line extraction amount control slurry oil.
5. heavy oil feedstock by contacting with high temperature catalyst, generates the reaction oil gas that is rich in C2, C3, C4 hydro carbons in the catalytic cracking reaction device.Generally greater than 500 ℃, if untimely these products are cooled off, heavy oil fraction wherein just may coking in feed-line when the reaction oil gas that is generated left reactor, thereby threatened the safe operation of device.The reaction oil gas of the present invention by making high potential temperature directly contacts with heavy charge as reaction raw materials, heat exchange, and the temperature that not only can reduce reaction oil gas in time prevents coking, can also make product obtain preliminary separation.Simultaneously, because the little amount of catalyst fine powder that carries in the reaction oil gas, can cold change to presort in the tower catalyst fines is washed in the heavy oil, make it at the bottom of the tower still is deposited to tower, discharge with slurry oil, thereby avoid catalyst fines obstruction or wear equipment and member in follow-up product separation process.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
The specific embodiment
(1) cold changing presorted tower
In the method for the invention, described cold changing presorted tower and mainly is made up of tower body and tower inner member.This tower is followed successively by tower still 1, cooling scrubbing section 2 and heat exchange fractionation zone 3 from bottom to top.Wherein, the height of described tower still accounts for this cold 5-20% that presorts the tower total height that changes, preferred 8-15%; The height of described cooling scrubbing section accounts for this cold 10-40% that presorts the tower total height that changes, preferred 12-35%; The height of described heat exchange fractionation zone accounts for this cold 40-80% that presorts the tower total height that changes, preferred 55-70%.
As shown in Figure 1, be provided with reaction oil gas inlet tube 4, slurry oil discharge pipe 5 and recycle oil extraction and return line 6 at the cold tower still of presorting tower that changes.The liquid level of tower still is higher than the reaction oil gas inlet tube.The slurry oil discharge pipe is arranged at the bottom of this tower still.
In the method for the invention, the top of described tower still is the cooling scrubbing section.Cool off the two-layer or two-layer above tower disc type inner member 10 that be arranged in parallel in the scrubbing section, two-layer above tower disc type inner member preferably is set.The concrete structure of described tower disc type inner member is referring to CN1485406A.Described tower disc type inner member is mainly by the baffle plate more than 2 groups or 2 groups and be arranged on the vertical partition plate of respectively organizing between the baffle plate and form, described every group of baffle plate by one group of inclination angle identical and baffle plate sheet that fixedly connected with vertical partition plate form.Preferably form described inner member, most preferably form described inner member by 3-9 group baffle plate by 2-16 group baffle plate.
Described every group of baffle plate is by one group of identical and baffle plate sheet composition that fixedly connected with vertical partition plate in inclination angle.Described inclination angle is the lower edge and the formed angle of horizontal direction of baffle plate sheet, and this angle should be 10-90 °, preferred 30-90 °.The present invention to the shape of described baffle plate sheet without limits, they both can be arcs, also can be dull and stereotyped, or by at an angle the flap that flat board constituted more than two or two.Horizontal range between each baffle plate sheet is the 0.1-5% of stripper internal diameter, preferred 0.5-4%.The length of baffle plate sheet is less than or equal to 1/2 of stripper internal diameter, and the height of baffle plate sheet is the 1-5% of stripper internal diameter, preferred 1.5-4.5%.Preferably suitably perforate on the described baffle plate sheet, its percent opening is 1-30%, preferred 3-25%.
Be provided with vertical partition plate between per two groups of baffle plates.The length of vertical partition plate is less than or equal to the internal diameter of stripper.The height of vertical partition plate is slightly less than or the vertical height of the baffle plate sheet that equals to be in tilted layout.
In order to make described inner member have higher intensity, can be along the arranged outside annular sidewall of this inner member.One side of each baffle plate sheet is fixedlyed connected with vertical partition plate, and opposite side is fixedlyed connected with annular sidewall or vertical partition plate.The present invention to described fixedly connected concrete mode without limits, welding, riveted joint etc. all can.The vertical height of annular sidewall is slightly larger than or the vertical height of the baffle plate sheet that equals to be in tilted layout.
The method to set up of described inner member is as follows: described inner member is horizontal positioned successively in the cooling scrubbing section, and the adjacent two layers inner member angle of inclination difference of corresponding baffle plate sheet mutually vertically.Like this, logistics is when flowing into lower floor's inner member by the upper strata inner member, and its flow direction changes.The quantity of set inner member requires to decide according to concrete engineering design, for example, and efficient of vertical height, cooling and the washing of cooling scrubbing section or the like.
The top of described tower disc type inner member is provided with liquid distributor 11, makes the petroleum hydrocarbon uniform distribution again after entering the cooling scrubbing section from the liquid state of heat exchange cooling zone, to improve cooling and the detersive efficiency for reaction oil gas.The present invention does not have special requirement for the structure of described liquid distributor, and any interior equally distributed distributor of liquid of tower that is applicable to all can use, for example, and V-shape orifice trough liquid distributor etc.
The top of described cooling scrubbing section is the heat exchange fractionation zone, and the packing section 12 in order to the raising fractionating efficiency more than two sections or two sections is set in the heat exchange fractionation zone.Described packing section is preferably selected structured packing for use, and for example, woven wire etc. are to reduce the pressure drop of tower.Suggestion correspondingly is provided with packing section according to the number of the set refluxing opening of heat exchange fractionation zone, extraction mouth.
Heat exchange fractionation zone of the present invention should be provided with at least that the extraction mouth 9 of heavy charge after the outlet 8 of 7, coolings of heavy charge inlet afterreaction oil gas, the heating, stage casing liquid phase are extracted out mouthful and refluxing opening.The porch of all liquid phase materials preferably is provided with liquid distributor, to guarantee the even distribution of liquid phase material in tower.The exit of taking out of all liquid phase materials preferably is provided with liquid trap 13, to prevent liquid phase material bias current takes place in tower.The present invention does not have specific (special) requirements for the design of liquid distributor and liquid trap, adopts the structural shape of this area routine to get final product.
(2) coldly change the logistics setting of presorting tower
The catalytic pyrolysis heavy charge enters cold changing as cooling medium from the top of heat exchange fractionation zone and presorts tower, and from the pyroreaction oil gas of catalytic pyrolysis process, comprise the atomizing steam that uses in the course of reaction, stripped vapor etc., enter cold changing by feed-line by the oil gas inlet tube that is positioned at the tower still and presort tower.Reaction oil gas and heavy charge are presorted counter current contacting in the tower cold changing, and realize heat transfer and mass transfer between two strands of materials.At the cooling scrubbing section, from the liquid phase hydrocarbon ils material of top heat exchange fractionation zone after liquid distributor evenly distributes, constantly changing flow direction in the process of flowing from top to bottom along the tower disc type inner member, with the reaction oil gas counter current contacting, the temperature of reaction oil gas is reduced, the catalyst granules that reaction oil gas is carried secretly washs to liquid phase hydrocarbon ils material simultaneously, and converges to the tower still with liquid phase hydrocarbon ils material.The liquid level of the liquid phase hydrocarbon ils material of tower still should be higher than the absolute altitude of reaction oil gas inlet tube.The liquid phase hydrocarbon ils material of tower still refluxes at the bottom of a part after the extraction at the bottom of the tower is as tower and is back to the top of cooling scrubbing section liquid distributor, and another part gets rid of outward as slurry oil.
At the heat exchange fractionation zone, by the counter current contacting of reaction oil gas and heavy charge, further reduce the temperature of reaction oil gas, and the heavy hydrocarbon oil cut condensation in the reaction oil gas is got off, enter in the liquid phase hydrocarbon ils material.Reaction oil gas is flowed through after each packing section of heat exchange fractionation zone, is drawn by the cold top of presorting tower of changing, and delivers to the subsequent product piece-rate system, further is separated into various products such as gasoline, diesel oil and gaseous hydrocarbon.At the heat exchange fractionation zone one or more mid-pumparound is set preferably, to take out unnecessary heat in the tower, vapour-liquid phase load in the compensation tower.The liquid phase hydrocarbon ils material that temperature has raise behind the above-mentioned heat exchange fractionation zone of flowing through is extracted out by the bottom of heat exchange fractionation zone, as the raw material of catalytic cracking reaction.
(3) the cold operating condition of presorting tower of changing
The cold operating pressure of presorting tower that changes is 0.1-0.35Mpa, preferred 0.15-0.30Mpa; Tower top temperature is 50-300 ℃, preferred 80-250 ℃; Column bottom temperature is 350-500 ℃, preferred 400-480 ℃; It is 300-400 ℃ that the heavy charge side line is extracted temperature out, preferred 320-380 ℃; It is 300-450 ℃ that temperature is extracted in intermediate reflux out, preferred 350-420 ℃; It is 150-320 ℃ that the tower temperature is returned in intermediate reflux, preferred 180-300 ℃.It is 500-800 ℃ that reaction oil gas is gone into the tower temperature, preferred 550-700 ℃; It is 30-130 ℃ that heavy oil feedstock is gone into the tower temperature, preferred 50-100 ℃.
Further specify method provided by the invention below in conjunction with accompanying drawing, but therefore the present invention is not subjected to any restriction.
The gas distributor of presorting the tower bottom by cooling from the pyroreaction oil gas that contains catalyst dust of catalytic cracking reaction device enters the tower still.Contact with the slurry oil in the tower still, heat exchange, the heavy component cooling liquation in the reaction oil gas enters in the slurry oil, the catalyst granules of carrying secretly in the reaction oil gas also is washed to slurry oil.A tower still slurry oil part is extracted out and is removed catalytic cracking regenerator, and the oil that acts as a fuel is to replenish the deficiency of catalytic cracking reaction heat, and a part turns back to cooling scrubbing section top after supercooling.The catalytic pyrolysis raw material (heavy charge) that comes from the tank field is introduced in the cold top of presorting tower of changing, and flows downward after liquid distributor distributes, and heavy charge directly contacts and is heated with the oil gas that rises in the process of flowing downward.The heavy charge of heat exchange fractionation zone of flowing through is heated to 200-400 ℃, is extracted out by the side line that is positioned at heat exchange fractionation zone bottom and mouthful extracts out, as the reaction feed of catalytic pyrolysis process.Reaction oil gas is progressively reducing temperature along should be cold changing in the process of presorting the tower rising, and the heavy component in the reaction oil gas becomes liquid phase through cooling, enters in the heavy charge of liquid phase.Rise to the cold reaction oil gas of presorting top of tower that changes and have been cooled to about 80-280 ℃, deliver to subsequent separation system, further be separated into various products.Below extracting mouth out, return in the tower middle and lower part of presorting tower heat exchange fractionation zone is extracted one liquid and cooling out from side line after cold changing, to take out heat unnecessary in the tower to guarantee heat balance.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Embodiment 1
This embodiment explanation: the implementation result of method provided by the present invention.
The reaction oil gas that is adopted in the process of the test and the composition of heavy charge see Table 1, and the cold main operating condition of presorting tower of changing is as follows: coldly change that to presort the column overhead temperature be 223 ℃, column bottom temperature is 452 ℃, and tower top pressure is 1.7bar, and tower bottom pressure is 1.9bar.The cold separating effect that changes sees Table 2.As can be seen from Table 2, adopt method provided by the invention can make the hydrocarbon mixture that is rich in low-carbon alkene obtain more satisfactory cooling and separating effect.
Table 1
| Logistics | Reaction oil gas | Heavy oil feedstock |
| Temperature, ℃ | 600 | 50 |
| Pressure, bar (A) | 2 | 2 |
| Molar flow, kmol/hr | 1904 | 256 |
| Mass flow kg/hr | 82000 | 82000 |
| Mass fraction | ||
| Hydrogen | 0.006 | 0 |
| Sulfur dioxide | 0.01 | 0 |
| Methane | 0.015 | 0 |
| Carbon dioxide | 0.001 | 0 |
| Ethene | 0.093 | 0 |
| Ethane | 0.008 | 0 |
| Propylene | 0.29 | |
| Propane | 0.017 | 0 |
| Isobutene | 0.07 | 0 |
| Butane | 0.07 | 0 |
| The 1-butylene | 0.05 | 0 |
| Steam | 0.06 | 0 |
| 40 ℃ of boiling ranges | 0.01 | 0 |
| 58 ℃ of boiling ranges | 0.004 | 0 |
| 72 ℃ of boiling ranges | 0.003 | 0 |
| 86 ℃ of boiling ranges | 0.003 | 0 |
| 100 ℃ of boiling ranges | 0.003 | 0 |
| 114 ℃ of boiling ranges | 0.004 | 0 |
| 128 ℃ of boiling ranges | 0.005 | 0 |
| 142 ℃ of boiling ranges | 0.005 | 0 |
| 156 ℃ of boiling ranges | 0.005 | 0 |
| 170 ℃ of boiling ranges | 0.006 | 0 |
| 184 ℃ of boiling ranges | 0.008 | 0 |
| 198 ℃ of boiling ranges | 0.013 | 0 |
| 211 ℃ of boiling ranges | 0.007 | 0 |
| 225 ℃ of boiling ranges | 0.006 | 0 |
| 239 ℃ of boiling ranges | 0.007 | 0 |
| 253 ℃ of boiling ranges | 0.007 | 0 |
| 267 ℃ of boiling ranges | 0.008 | 0 |
| 281 ℃ of boiling ranges | 0.008 | 0 |
| 295 ℃ of boiling ranges | 0.008 | 0 |
| 308 ℃ of boiling ranges | 0.007 | 0 |
| 319 ℃ of boiling ranges | 0.003 | 0 |
| 338 ℃ of boiling ranges | 0.004 | 0.036 |
| 351 ℃ of boiling ranges | 0.011 | 0.103 |
| 364 ℃ of boiling ranges | 0.013 | 0.119 |
| 378 ℃ of boiling ranges | 0.012 | 0.109 |
| 392 ℃ of boiling ranges | 0.011 | 0.104 |
| 406 ℃ of boiling ranges | 0.013 | 0.114 |
| 420 ℃ of boiling ranges | 0.01 | 0.094 |
| 440 ℃ of boiling ranges | 0.021 | 0.195 |
| 467 ℃ of boiling ranges | 0.021 | 0.126 |
| 497 ℃ of boiling ranges | 0.02 | 0 |
| 522 ℃ of boiling ranges | 0.014 | 0 |
| 554 ℃ of boiling ranges | 0.021 | 0 |
| 574 ℃ of boiling ranges | 0.008 | 0 |
| Add up to | 1.000 | 1.000 |
Table 2
| Logistics | Raw material is extracted out | Slurry oil | Cat head |
| Temperature ℃ | 339.9 | 452.4 | 223.6 |
| Pressure bar (A) | 1.782 | 1.9 | 1.7 |
| Molar flow rate, kmol/hr | 253.704 | 13.076 | 1839.98 |
| Mass flowrate, kg/hr | 82000 | 8729.0 | 73271.0 |
| Mass fraction, % | |||
| H2 | 0 | 0 | 0.007 |
| H2S | 0 | 0 | 0.011 |
| CH4 | 0 | 0 | 0.017 |
| CO2 | 0 | 0 | 0.001 |
| C2H4 | 0 | 0 | 0.103 |
| C2H6 | 0 | 0 | 0.009 |
| C3H6 | 0 | 0 | 0.322 |
| C3H8 | 0 | 0 | 0.019 |
| i-C4H8 | 0 | 0 | 0.078 |
| C4H10 | 0 | 0 | 0.078 |
| 1-C4H8 | 0 | 0 | 0.055 |
| H2O | 0 | 0 | 0.066 |
| 40 ℃ of boiling ranges | 0 | 0 | 0.011 |
| 58 ℃ of boiling ranges | 0 | 0 | 0.005 |
| 72 ℃ of boiling ranges | 0 | 0 | 0.003 |
| 86 ℃ of boiling ranges | 0 | 0 | 0.004 |
| 100 ℃ of boiling ranges | 0 | 0 | 0.004 |
| 114 ℃ of boiling ranges | 0 | 0 | 0.005 |
| 128 ℃ of boiling ranges | 0 | 0 | 0.005 |
| 142 ℃ of boiling ranges | 0 | 0 | 0.006 |
| 156 ℃ of boiling ranges | 0 | 0 | 0.006 |
| 170 ℃ of boiling ranges | 0 | 0 | 0.006 |
| 184 ℃ of boiling ranges | 0 | 0 | 0.009 |
| 198 ℃ of boiling ranges | 0 | 0 | 0.014 |
| 211 ℃ of boiling ranges | 0 | 0 | 0.008 |
| 225 ℃ of boiling ranges | 0 | 0 | 0.007 |
| 239 ℃ of boiling ranges | 0 | 0 | 0.007 |
| 253 ℃ of boiling ranges | 0 | 0 | 0.007 |
| 267 ℃ of boiling ranges | 0 | 0 | 0.008 |
| 281 ℃ of boiling ranges | 0.001 | 0 | 0.008 |
| 295 ℃ of boiling ranges | 0.001 | 0 | 0.008 |
| 308 ℃ of boiling ranges | 0.001 | 0 | 0.006 |
| 319 ℃ of boiling ranges | 0.001 | 0 | 0.002 |
| 338 ℃ of boiling ranges | 0.013 | 0 | 0.029 |
| 351 ℃ of boiling ranges | 0.081 | 0 | 0.035 |
| 364 ℃ of boiling ranges | 0.115 | 0 | 0.016 |
| 378 ℃ of boiling ranges | 0.111 | 0.001 | 0.007 |
| 392 ℃ of boiling ranges | 0.109 | 0.001 | 0.004 |
| 406 ℃ of boiling ranges | 0.121 | 0.001 | 0.003 |
| 420 ℃ of boiling ranges | 0.1 | 0.001 | 0.001 |
| 440 ℃ of boiling ranges | 0.21 | 0.004 | 0.001 |
| 467 ℃ of boiling ranges | 0.133 | 0.138 | 0 |
| 497 ℃ of boiling ranges | 0 | 0.273 | 0 |
| 522 ℃ of boiling ranges | 0 | 0.197 | 0 |
| 554 ℃ of boiling ranges | 0 | 0.28 | 0 |
| 574 ℃ of boiling ranges | 0 | 0.104 | 0 |
| Add up to | 1.000 | 1.000 | 1.000 |
Comparative Examples
What this Comparative Examples adopted is conventional catalytic cracking main fractionating tower, and the composition of reaction oil gas is identical with embodiment 1, and the main operating condition of FCC main fractionating tower sees Table 3.Because catalytic cracking reaction oil gas temperature is high and be rich in the C2-C4 cut, cause the via hole linear speed of column plate in the fractionating column too big, make fractionating column be in the liquid flooding state, fluctuation of service can't carry out normal separation.
Table 3
| The fractionating column size | Φ3800*46284 | Column bottom temperature, ℃ | 480 |
| Tower top temperature, ℃ | 260 | The cat head percent opening | 11％ |
| Tower top pressure, MPa (g) | 0.15 | The via hole linear speed, m/s | 17.64 |
Embodiment 2
The reaction oil gas that present embodiment adopted is identical with embodiment 1 with the composition of heavy charge, the cold main operating condition of presorting tower of changing is as follows: coldly change that to presort the column overhead temperature be 95.6 ℃, column bottom temperature is 347 ℃, and tower top pressure is 200KPa, and tower bottom pressure is 201KPa.The cold separating effect that changes sees Table 4.As can be seen from Table 4, adopt method provided by the invention can realize being rich in the refrigerated separation of low-carbon alkene petroleum hydrocarbon effectively.
Table 4
| Logistics | Raw material is extracted out | Slurry oil | Cat head |
| Temperature ℃ | 209 | 347 | 95.6 |
| Molar flow rate kmol/hr | 102.57 | 8.91 | 724.1 |
| Mass fraction, % | |||
| Methane | 0 | 0 | 2.0653 |
| Propane | 0 | 0 | 9.1508 |
| Ethane | 0 | 0 | 1.3596 |
| Ethene | 0 | 0 | 9.1865 |
| Propylene | 0 | 0 | 36.4927 |
| Butane | 0 | 0 | 4.141 |
| Maleic | 0 | 0 | 1.8128 |
| The 1-butylene | 0 | 0 | 2.0771 |
| Anti-butylene | 0 | 0 | 3.4477 |
| Iso-butane | 0 | 0 | 3.423 |
| Hydrogen | 0 | 0 | 0.3798 |
| 57 of boiling ranges | 0 | 0 | 3.971 |
| 137 of boiling ranges | 0 | 0 | 1.4817 |
| 162 of boiling ranges | 0 | 0 | 1.3801 |
| 187 of boiling ranges | 2.42E-04 | 0 | 1.4899 |
| 212 of boiling ranges | 5.34E-04 | 0 | 1.7761 |
| 237 of boiling ranges | 1.01E-03 | 0 | 1.8299 |
| 262 of boiling ranges | 1.76E-03 | 0 | 1.7475 |
| 287 of boiling ranges | 3.09E-03 | 0 | 1.677 |
| 312 of boiling ranges | 5.52E-03 | 0 | 1.6316 |
| 337 of boiling ranges | 0.0106 | 0 | 1.6774 |
| 363 of boiling ranges | 0.0243 | 1.55E-03 | 1.974 |
| 387 of boiling ranges | 0.0609 | 2.78E-03 | 2.2912 |
| 413 of boiling ranges | 0.3347 | 6.57E-03 | 3.2539 |
| 435 of boiling ranges | 0.6289 | 2.63E-03 | 0.2355 |
| 457 of boiling ranges | 0.5322 | 2.47E-03 | 1.57E-03 |
| 492 of boiling ranges | 0.0291 | 2.50E-04 | 6.47E-08 |
| 522 of boiling ranges | 0.1873 | 5.49E-04 | 5.77E-03 |
| 540 of boiling ranges | 1.1147 | 1.19E-03 | 0.022 |
| 567 of boiling ranges | 1.1795 | 3.07E-03 | 8.69E-03 |
| 593 of boiling ranges | 1.2094 | 5.29E-03 | 3.65E-03 |
| 616 of boiling ranges | 1.2227 | 7.77E-03 | 1.71E-03 |
| 639 of boiling ranges | 1.9751 | 0.0116 | 1.30E-03 |
| 664 of boiling ranges | 3.9114 | 0.0175 | 1.16E-03 |
| 688 of boiling ranges | 4.5166 | 0.025 | 6.09E-04 |
| 712 of boiling ranges | 4.3032 | 0.0358 | 2.52E-04 |
| 737 of boiling ranges | 4.1987 | 0.0548 | 1.05E-04 |
| 762 of boiling ranges | 4.4983 | 0.099 | 4.81E-05 |
| 787 of boiling ranges | 5.715 | 0.2343 | 2.59E-05 |
| 825 of boiling ranges | 12.7102 | 2.0226 | 1.56E-05 |
| 874 of boiling ranges | 19.5561 | 13.0539 | 0 |
| 930 of boiling ranges | 29.5728 | 67.745 | 0 |
| 971 of boiling ranges | 2.4955 | 15.7647 | 0 |
| 1019 of boiling ranges | 2.66E-04 | 0.8991 | / |
Claims (12)
1, a kind of separation method of hydrocarbon reaction oil gas, it is characterized in that: the catalytic cracking reaction oil gas that is rich in the C2-C4 hydro carbons enters cold the changing that comprises tower still, cooling scrubbing section and heat exchange fractionation zone by the bottom and presorts in the tower, with the catalytic pyrolysis heavy charge counter current contacting of being injected by this top of tower; Reduce the temperature of reaction oil gas, the catalyst granules that removes in the reaction oil gas to be carried secretly at tower still and cooling scrubbing section; Progressively reduce the temperature of reaction oil gas and make under the heavy ends condensation in the reaction oil gas at the heat exchange fractionation zone and enter in the heavy charge; Reaction oil gas after the cooling is delivered to subsequent separation system through this cold top of presorting tower of changing; The heavy charge temperature that in the process that flows downward along the heat exchange fractionation zone, progressively raises, and behind the heat exchange fractionation zone of flowing through, be drawn out of, deliver to catalytic cracking reaction device or hydrotreating reactor as feedstock oil.
2,, it is characterized in that described cold changing presort tower and be followed successively by tower still, cooling scrubbing section and heat exchange fractionation zone from bottom to top according to the method for claim 1; The height of described tower still accounts for this cold 5-20% that presorts the tower total height that changes, and the height of described cooling scrubbing section accounts for this cold 10-40% that presorts the tower total height that changes, and the height of described heat exchange fractionation zone accounts for this cold 40-80% that presorts the tower total height that changes.
3,, it is characterized in that the height of described tower still accounts for this cold 8-15% that presorts the tower total height that changes according to the method for claim 2; The height of described cooling scrubbing section accounts for this cold 12-35% that presorts the tower total height that changes; The height of described heat exchange fractionation zone accounts for this cold 55-70% that presorts the tower total height that changes.
4, according to the method for claim 1, two-layer or two-layer above tower disc type inner member is characterized in that be arrangeding in parallel in the described cooling scrubbing section.
5, according to the method for claim 4, it is characterized in that described tower disc type inner member mainly by the baffle plate more than 2 groups or 2 groups and be arranged on the vertical partition plate of respectively organizing between the baffle plate and form, described every group of baffle plate by one group of inclination angle identical and baffle plate sheet that fixedly connected with vertical partition plate form.
6, according to the method for claim 4, it is characterized in that described inner member horizontal positioned successively in the cooling scrubbing section, and the adjacent two layers inner member angle of inclination difference of corresponding baffle plate sheet mutually vertically.
7,, it is characterized in that the top of described tower disc type inner member is provided with liquid distributor according to the method for claim 4.
8,, it is characterized in that being provided with in the described heat exchange fractionation zone the packing section more than two sections or two sections in order to the raising fractionating efficiency according to the method for claim 1.
9,, it is characterized in that described heat exchange fractionation zone is provided with at least that the extraction mouth of heavy charge after the outlet of heavy charge inlet, a cooling afterreaction oil gas, the heating, stage casing liquid phase are extracted out mouthful and refluxing opening according to the method for claim 1.
10, according to the method for claim 1, it is characterized in that the described cold operating pressure of presorting tower that changes is 0.1-0.35Mpa, tower top temperature is 50-300 ℃, column bottom temperature is 350-500 ℃, it is 300-400 ℃ that the heavy charge side line is extracted temperature out, and it is 300-450 ℃ that temperature is extracted in intermediate reflux out, and it is 150-320 ℃ that the tower temperature is returned in intermediate reflux, it is 500-800 ℃ that reaction oil gas is gone into the tower temperature, and it is 30-130 ℃ that heavy oil feedstock is gone into the tower temperature.
11, according to the method for claim 10, it is characterized in that the described cold operating pressure of presorting tower that changes is 0.15-0.30Mpa, tower top temperature is 80-250 ℃, and column bottom temperature is 400-480 ℃, it is 320-380 ℃ that the heavy charge side line is extracted temperature out, and it is 350-420 ℃ that temperature is extracted in intermediate reflux out; It is 180-300 ℃ that the tower temperature is returned in intermediate reflux, and it is 550-700 ℃ that reaction oil gas is gone into the tower temperature, and it is 50-100 ℃ that heavy oil feedstock is gone into the tower temperature.
12, according to the method for claim 1, it is characterized in that the described cold middle and lower part of presorting tower heat exchange fractionation zone of changing extracts one liquid out from side line, after cooling off, below extracting out mouthful, return in the tower.
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| CNB2004100862245A CN100363076C (en) | 2004-10-28 | 2004-10-28 | Separation method of hydrocarbon reaction oil gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101294104B (en) * | 2008-06-05 | 2012-02-01 | 华东理工大学 | Hydrocracking recycle hydrogen deoiling, dewatering separation method and apparatus |
| CN101684058B (en) * | 2008-09-27 | 2013-01-09 | 中国石油化工股份有限公司 | Utilization method of noncondensable gas generated by alkylaromatic hydrocarbon isomerization |
| CN111321004A (en) * | 2020-03-31 | 2020-06-23 | 中国石油化工股份有限公司 | Oil slurry circulating heat-extracting system of catalytic cracking fractionating tower |
| CN113396202A (en) * | 2019-02-07 | 2021-09-14 | 埃克森美孚化学专利公司 | Primary fractionator with reduced fouling |
| CN116747547A (en) * | 2023-08-22 | 2023-09-15 | 齐齐哈尔黎明气体有限公司 | Emptying gas recovery device in propane gas supply process |
| CN111321004B (en) * | 2020-03-31 | 2024-06-11 | 中国石油化工股份有限公司 | Catalytic cracking fractionating tower slurry oil circulation heat-taking system |
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| US6271433B1 (en) * | 1999-02-22 | 2001-08-07 | Stone & Webster Engineering Corp. | Cat cracker gas plant process for increased olefins recovery |
| CN1100851C (en) * | 2000-04-29 | 2003-02-05 | 中国石化集团洛阳石油化工工程公司 | Suddenly cooling tower and process of resultant from fluidized catalytic transform reaction of hydrocarbons |
| CN1191111C (en) * | 2002-09-28 | 2005-03-02 | 中国石油化工股份有限公司 | Inner component of tower disc type catalytic cracking stripping equipment |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101294104B (en) * | 2008-06-05 | 2012-02-01 | 华东理工大学 | Hydrocracking recycle hydrogen deoiling, dewatering separation method and apparatus |
| CN101684058B (en) * | 2008-09-27 | 2013-01-09 | 中国石油化工股份有限公司 | Utilization method of noncondensable gas generated by alkylaromatic hydrocarbon isomerization |
| CN113396202A (en) * | 2019-02-07 | 2021-09-14 | 埃克森美孚化学专利公司 | Primary fractionator with reduced fouling |
| CN111321004A (en) * | 2020-03-31 | 2020-06-23 | 中国石油化工股份有限公司 | Oil slurry circulating heat-extracting system of catalytic cracking fractionating tower |
| CN111321004B (en) * | 2020-03-31 | 2024-06-11 | 中国石油化工股份有限公司 | Catalytic cracking fractionating tower slurry oil circulation heat-taking system |
| CN116747547A (en) * | 2023-08-22 | 2023-09-15 | 齐齐哈尔黎明气体有限公司 | Emptying gas recovery device in propane gas supply process |
| CN116747547B (en) * | 2023-08-22 | 2023-10-24 | 齐齐哈尔黎明气体有限公司 | Emptying gas recovery device in propane gas supply process |
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