CN1782023A - Separating method for hydrocarbon oil catalytic cracking reaction products - Google Patents
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Abstract
The process of separating the hydrocarbon oil catalytically cracking reaction products includes: introducing oil gas as the catalytically cracking reaction products to the bottom of cold exchange pre-separating tower for counter flow contact with catalytically cracked material from the tower top to lower temperature, leading out heavy components and entrained catalyst powder together with oil slurry from the tower bottom, leading out the catalytically cracked material via side line and extracting light oil fraction and other gas material from the tower top; cooling and separating the material extracted from the top of the pre-separating tower in a triphase separator to obtain gaseous material flow, which is compressed and separated in subsequent unit to produce condensate separated in rectifying tower, and sewage feeding for treatment in a sewage treating system. The present invention can realize effective separation of reacted hydrocarbon oil gas.
Description
Technical field
The present invention relates to the separation method of catalytic cracking reaction products, specifically, is a kind of separation method of catalytic cracking reaction products of the C2-C4 of being rich in hydro carbons.
Background technology
The traditional method of the petroleum hydrocarbon system of utilization ethene, propylene is a steam splitting process, and applicable raw materials is ethane, Sweet natural gas, petroleum naphtha or solar oil.But the heavy and oily shortage of lightweight material along with the change of stock oil utilizes heavy feed stock to produce low-carbon alkene by the method for catalytic cracking, has become a kind of trend of development.
CN1069016A discloses a kind of catalysis conversion method that utilizes the heavy crude hydro carbons to produce low-carbon alkene.This method is selected solid acid type catalyzer for use, is under the condition of 5-35 at temperature of reaction 650-900 ℃, agent-oil ratio, and the productive rate of its ethene+propylene+butylene can reach 30-40m%.CN1083092A discloses a kind of method of similar petroleum hydrocarbon preparing low-carbon olefin by catalytically cracking, and its temperature of reaction is 680-780 ℃.Its significant process characteristic of method that adopts fluid catalytic cracking to produce low-carbon alkene is: the temperature of reaction height, agent-oil ratio is big, the reaction times is short etc.Because the temperature of reaction of preparing low-carbon olefin by catalytically cracking is 600-900 ℃, its cracking severity is big, gas yield is more than 50% in the product, substantially exceed conventional catalytic cracking gas productive rate (conventional catalytic cracking gas productive rate is about 20%), how reaction product effectively being separated is a very real problem.
For typical catalytic cracking FCC technology separation system, reaction oil gas enters the separation column bottom, is divided into different intermediates at separation column, and cat head is a raw gasline, and side line has diesel oil and freshening wet goods.The gasoline of cat head further separates through absorbing to stablize with rich gas, behind diesel oil process stripping, the cooling heat transferring, goes out device as finished product.
CN1160748A has announced a kind of separation method that is rich in the catalyzed conversion product of propylene, butylene, is characterized in making crackate to enter separation column, extracts the mixture of recycle stock and slurry oil at the bottom of the tower out, and with it directly as the thermal source of stabilizer reboiler.The separation column mid-pumparound is as taking off the thermal source of receiving the tower reboiler.
CN1100851C discloses a kind of quench tower and quick cooling method of hydro carbons fluidisation catalytic conversion reaction product.Described quench tower is followed successively by gas phase separation district, chilling heat transfer and catalyst dust washing section, liquid level control region from top to bottom.This quench tower can directly be located at the settling vessel top and combine as a whole with settling vessel, also can independently be built in the position near settling vessel.Described quick cooling method is contact heat-exchanging in quench tower with reaction oil gas and quenching oil, and 670-730 ℃ reaction oil gas is cooled to about 300-400 ℃, carries out later separation then.
" ethene engineering " provided the separation process of preparing ethylene by steam cracking.Pyrolyzer outlet Pintsch process gas in the distillate cracker is behind the waste heat boiler recovered energy, again about quencher uses the quenching oil spraying cooling to 220-230 ℃.Cooled splitting gas enters oil scrubber, and cat head sprays with pyrolysis gasoline, and tower top temperature is controlled at about 100-110 ℃, guarantees that the moisture in the splitting gas is taken out of from cat head.The liquid phase hydro carbons part that the tower still is extracted out is condensed into product oil, and a part reclaims heat as the thermal source of dilution steam generation.Deliver to chilling spray column cooling reacted gas through steam dilution system refrigerative quenching oil major part.The liquefied gas at oil scrubber top enters water wash column, and cat head carries out spray washing with quenched water, and cat head splitting gas temperature is reduced to 40 ℃, enters cracking gas compressor.The tower still fractionates out moisture and pyrolysis gasoline.Tower still oil-water mixture separates water outlet and gasoline through water-and-oil separator.
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 stage compression and cooling, with C3 and C3
+Separate C3
+Through isolating C4 and gasoline fraction behind stripping tower and the stabilizer tower.The C3 cut is through refining, dry, enters follow-up low temperature separation process system, and through demethanizing tower, deethanizing column and depropanizing tower, ethene separates with propylene the most at last.
In sum, because the catalytic pyrolysis gas production rate is big, reaction oil gas temperature height, be subjected to the restriction of interior gas phase linear speed of tower and thermal load, the separation process of conventional FCC main fractionating tower has been difficult to adapt to this separation requirement.Owing to contain solid catalyst particle in the heaviness of cracking stock and the splitting gas, therefore the separation process of traditional preparing ethylene by steam cracking is not suitable for the preparing low-carbon olefin by catalytically cracking technological process yet.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of separation to be rich in the method for the catalytic cracking reaction products of C2-C4 hydrocarbon and light aromatic hydrocarbons, with the separation of the hydrocarbon reaction oil gas that solves high temperature, high gas content and entrained catalyst dust.
Method provided by the invention may further comprise the steps: the reaction oil gas 101 of (1) autocatalysis in the future cracking reactor is introduced the cold bottom of presorting tower 1 of changing, and inject catalytic pyrolysis raw material 102 by this top of tower, the catalytic pyrolysis raw material in the process that flows downward with mobile reaction oil gas counter current contact upwards and be heated; Reaction oil gas stream temperature in the process of flowing that makes progress constantly reduces, heavy constituent wherein and the catalyst dust of being carried secretly enter the tower bottom branch and draw with slurry oil at the bottom of the tower 104, the catalytic pyrolysis raw material is drawn through side line 103, and light oil distillate and remaining gas stream 105 are extracted out from cat head; (2) from cold change to presort to send into the triphase separator 3 after logistics 105 coolings that column overhead extracts out separate, after boosting, the gaseous stream 108 compressed machines that obtain after the separation deliver to follow-up gas separation unit, the condensed liquid 111 that phlegma 109 that obtains after the separation and gaseous stream 108 produce after compression converges to be sent into rectifying tower 2 for logistics 131 and separates, and the sewage 110 that obtains after the separation send Sewage treatment systems.
Compared with prior art, the method for the invention mainly has the beneficial effect of following several respects:
1. catalytic cracking reaction products is C2, C3 alkene and BTX, and all the other products are sent the reactor cracking back to again as raw material, can make the catalytic pyrolysis raw material except that the small part combustion oil, all is converted into low-carbon alkene and light aromatic hydrocarbons, does not produce gasoline and diesel oil.
2. heavy oil feedstock and reaction product are presorted direct heat exchange in the tower cold changing, can make reaction oil gas cooling rapidly in a short period of time on the one hand, simultaneously raw material cold change to presort be heated directly to the required temperature of hydrogenation reaction in the tower, needn't establish raw materials furnace and heating in addition, reduced equipment, simplified flow process, Btu utilization fully, rationally.
3. unreacted diesel oil distillate and heavy oil fraction presort cold changing that condensation becomes liquid phase in the tower, come along hydrogenator with heavy feed stock, have played the prefractionation effect.The heavy oil 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.
4. heavy distillate can be used as combustion oil and directly sprays into the revivifier use in the reaction oil gas, to replenish the required heat of catalytic cracking reaction, simultaneously also can be according to the heat balance of revivifier, by regulating the output of side line extraction amount control slurry oil, make unnecessary slurry oil enter hydrogenator, behind hydrogenation as the raw material of catalytic cracking reaction device, or directly as the raw material of catalytic pyrolysis.
5. rectifying tower 2 is operated under higher pressure, can guarantee that cat head uses water as heat-eliminating medium.Working pressure 0.5≤p≤the 1.6MPA (cutting off) of rectifying tower 2 generally speaking, under appropriate condition, rectifying tower 2 also can be operated outside above-mentioned pressure range.
6. first side line (middle and upper part) of rectifying tower 2 is extracted out in the stream and is mainly C 4 fraction, is the desirable feedstock of producing C2/C3 alkene, can be directly after gas separation unit is told wherein C3 or behind hydrogenation as the raw material use of catalytic cracking reaction device.
7. second side line (middle and lower part) of rectifying tower 2 is extracted out in the stream and is mainly light naphthar, wherein contain a large amount of light aromatic hydrocarbons (benzene,toluene,xylene), can be directly as the unitary charging of extracting reclaiming triphen wherein, raffinate can be with the C 4 fraction of first side line raw material as the catalytic cracking reaction device.
Description of drawings
Fig. 1-the 4th, the schematic flow sheet of separation method of the present invention.
Embodiment
Separation method of the present invention mainly comprises: cold changing presorted tower 1, rectifying tower 2, triphase separator 3, catalyst cracker 4, revivifier 5, hydrogenator 6 and corresponding heat-exchange equipment, pump, and Fig. 1 to 4 is seen in its technical process.
In method provided by the present 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, cooling washing section and heat exchange fractionation zone 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 washing 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%.Be provided with reaction oil gas inlet tube, slurry oil vent pipe and turning oil extraction and return line 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 vent pipe is arranged at the bottom of this tower still.The relevant cold more detailed description of presorting tower of changing sees also Chinese patent application 200410086224.5.
Separation method provided by the present invention can be described in detail as follows: the high-temperature oil gas that contains catalyst dust 101 of being come out by the catalytic cracking reaction device directly is introduced in the cold bottom of presorting tower 1 of changing.Catalytic pyrolysis raw material (or the oily raw material of weighing) 102 that comes from the tank field introduced and flowed downward by the cold top of presorting tower of changing, and heavy oil feedstock directly contacts and is heated with the oil gas that rises in the process of flowing downward.Extract a mouthful extraction out by the side line of this tower when heavy oil feedstock is heated to about 300-400 ℃, side line is extracted logistics 103 out as shown in the figure.Heavy oil feedstock after being heated can also can be introduced into hydrogenator 6 and carry out the hydrogenation pre-treatment directly as the raw material of cat-cracker, and then as the raw material of cat-cracker.Presort the oil gas that enters at the bottom of the Tata and uphill process, constantly reduce stream temperature and be condensed and separate from cold changing.The little amount of catalyst dust of carrying secretly in heavy constituent wherein and the oil gas is washed by defluent heavy oil feedstock and draws with slurry oil at the bottom of the tower 104; The cut suitable with the heavy oil feedstock boiling range, for example heavy gas oil cut etc. is drawn from side line 103 with heavy oil feedstock.Light oil distillate, for example, gasoline fraction and/or part solar oil cut and other gaseous stream are cooled in uphill process about 120-280 ℃ to be extracted out from the top as overhead product 105.Described cold changing presorted tower one or more mid-pumparound is set, promptly, extract liquid 106 more than one or one out from the cold middle and lower part side line of presorting tower that changes, cooled logistics 107 is from extracting out mouthful following or extracting out mouthful above or the extraction mouth returns in the tower, to take out heat unnecessary in the tower, to guarantee heat balance, cooled logistics 107 is returned in the tower below extracting mouth out.
From the gaseous stream 105 that cat head is extracted out, contain the following cut of whole C4, almost whole gasoline fractions and water, at first be cooled to normal temperature (below 40 ℃), enter into triphase separator 3 then gas stream 108, phlegma 109 and water 110 are separated.Gaseous stream 118 after gas stream 108 compressed machines boost is delivered to gas separation unit, and water 110 send Sewage treatment systems, and the condensed liquids 111 that phlegma 109 and 108 compression backs produce merge into logistics 131 usefulness and are pumped into rectifying tower 2 and separate.
In the method for the invention, the cold working pressure of presorting tower that changes is 0.1-0.35MPa (cutting off), preferred 0.15-0.25MPA (cutting off); Service temperature is cat head 100-280 ℃, and preferred 120-250 ℃, service temperature is 350-500 ℃ at the bottom of the tower, and preferred 380-480 ℃, the temperature that side line is extracted logistics 103 out is 300-400 ℃, preferred 320-380 ℃; The temperature that logistics 106 is extracted in mid-pumparound out is 300-450 ℃, and preferred 350-420 ℃, the temperature of return logistics 107 is 120-280 ℃, preferred 150-250 ℃.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 ℃.
For guarantee rectifying tower 2 tops can water as heat-eliminating medium, should make this column overhead maintain higher temperature, generally be not less than 30 ℃.Rectifying tower 2 is preferably in operation under the higher pressure, and the working pressure of advising rectifying tower 2 generally speaking is 0.5-1.6MPA (cutting off), but is not limited to this scope, and under appropriate condition, rectifying tower 2 also can be operated outside above-mentioned pressure range.The cat head service temperature is 10-60 ℃, preferred 20-50 ℃; It is 30-120 ℃ that first side-stream 114 is extracted temperature out, preferred 50-90 ℃; It is 80-300 ℃ that second side line 115 is extracted temperature out, preferred 100-200 ℃; Service temperature is 200-450 ℃ at the bottom of the tower, preferred 250-400 ℃.
The following examples will give further instruction to method provided by the present invention, but therefore the present invention is not subjected to any restriction.
Embodiment
This embodiment explanation: logistics separates the resulting result in back to catalytic cracking reaction to adopt separation method of the present invention.
Involved catalytic cracking reaction oil gas among the embodiment, be that the character of logistics 101 and the character and the main operating parameters of main operating parameters and heavy oil feedstock 102 see Table 1, cold main operational condition such as the table 2 of presorting tower and rectifying tower that change, the composition of the product stream that obtains after separation process fractionation of the present invention and character see Table 3 and table 4.
The separation process that present embodiment adopted as shown in Figure 2.Main operational steps is as follows: be introduced in from the high-temperature oil gas 101 of catalytic cracking reaction device and coldly change the bottom of presorting tower 1, and catalytic pyrolysis heavy oil feedstock 102 is introduced by the top of this tower.When being heated to 350-380 ℃, heavy oil feedstock extracts a mouthful extraction out, as the raw material of cat-cracker by side line.Reaction oil gas is constantly lowered the temperature in the process that rises along this tower and is condensed and separates.The little amount of catalyst dust of carrying secretly in heavy constituent wherein and the oil gas is washed down and draws with slurry oil at the bottom of the tower 104; The cuts suitable with the heavy oil feedstock boiling range such as heavy gas oil cut are drawn from side line 103.Gasoline fraction is cooled in uphill process about 200-250 ℃ with part solar oil cut and other gaseous stream and extracts out from the top.Extract one liquid 106 and cooling back from side line out and return in the tower 107 below extract out mouthful in the cold middle and lower part of presorting tower of changing, to take out heat unnecessary in the tower, to guarantee heat balance.From the gaseous stream 105 that cat head is extracted out, contain the following cut of whole C4, almost whole gasoline fractions and water, at first be cooled to below 40 ℃, enter then in the triphase separator 3 gas stream 108, phlegma 109 and water 110 are separated.Gaseous stream 118 after gas stream 108 compressed machines boost is delivered to gas separation unit, and water 110 send Sewage treatment systems, and the condensed liquids 111 that phlegma 109 and 108 compression backs produce merge into logistics 131 and deliver to rectifying tower 2 and separate.Logistics 131 in rectifying tower 2, be separated into overhead gas logistics 113 based on the following cut of C3, based on first side line of C3, C 4 fraction extract logistics 114 out, based on second side line extraction logistics 115 of gasoline fraction, based on the tower base stream 117 of heavy petrol and diesel oil distillate.Wherein, gaseous stream after logistics 113 and logistics 108 compressions merges into the 116 body separating units that degas, first side line is extracted logistics 114 out and is delivered to follow-up C 3/C4 separation column, extract logistics 115 out based on second side line of gasoline fraction and deliver to aromatic hydrocarbons extracting unit, raffinate 119 and heavy constituent 117 are sent the catalytic cracking reaction device back to and are reacted.
Effectively separated by the catalytic cracking reaction oil gas of showing 3-4 as can be seen, adopt method provided by the invention to make to be rich in low-carbon alkene.
Table 1
| The | 101 | 102 |
| Temperature, ℃ | 600 | 50 |
| Pressure, bar (a) | 2 | 2 |
| Molar flow rate, kmol/hr | 1890.77 | 221.68 |
| Mass flow rate, kg/hr | 80,000 | 80,000 |
| Massfraction | ||
| H2 | 0.0060 | 0 |
| H2S | 0.0100 | 0 |
| CH4 | 0.0150 | 0 |
| CO2 | 0.0010 | 0 |
| C2H4 | 0.0931 | 0 |
| C2H6 | 0.0080 | 0 |
| C3H6 | 0.2903 | 0 |
| C3H8 | 0.0170 | 0 |
| i-C4H8 | 0.0701 | 0 |
| C4H10 | 0.0701 | 0 |
| 1-C4H8 | 0.0501 | 0 |
| H20 | 0.0601 | 0 |
| 32℃ | 0.0230 | 0 |
| 58℃ | 0.0050 | 0 |
| 73℃ | 0.0050 | 0 |
| 86℃ | 0.0060 | 0 |
| 100℃ | 0.0060 | 0 |
| 114℃ | 0.0070 | 0 |
| 128℃ | 0.0080 | 0 |
| 142℃ | 0.0080 | 0 |
| 156℃ | 0.0080 | 0 |
| 170℃ | 0.0090 | 0 |
| 184℃ | 0.0120 | 0 |
| 198℃ | 0.0170 | 0 |
| 212℃ | 0.0190 | 0 |
| 224℃ | 0.0110 | 0 |
| 239℃ | 0.0070 | 0 |
| 253℃ | 0.0080 | 0 |
| 267℃ | 0.0080 | 0 |
| 281℃ | 0.0080 | 0 |
| 295℃ | 0.0080 | 0 |
| 309℃ | 0.0090 | 0 |
| 322℃ | 0.0090 | 0 |
| 336℃ | 0.0070 | 0 |
| 349℃ | 0.0030 | 0.0130 |
| 366℃ | 0.0050 | 0.0700 |
| 378℃ | 0.0060 | 0.0900 |
| 392℃ | 0.0050 | 0.0820 |
| 406℃ | 0.0050 | 0.0840 |
| 420℃ | 0.0050 | 0.0840 |
| 442℃ | 0.0140 | 0.1710 |
| 469℃ | 0.0180 | 0.1570 |
| 496℃ | 0.0190 | 0.1670 |
| 523℃ | 0.0140 | 0.0800 |
| ＞547℃ | 0.0070 | 0.0020 |
| SUM | 1.0000 | 1.0000 |
Table 2
| Cold changing presorted tower | ||
| Temperature | Pressure | |
| Unit | ℃ | bar |
| Cat head | 224 | 1.7 |
| At the bottom of the tower | 452 | 1.9 |
| Rectifying tower | ||
| Temperature | Pressure | |
| Unit | ℃ | bar |
| Cat head | 28 | 13 |
| At the bottom of the tower | 375 | 13.5 |
Table 3
| The | 103 | 104 | 105 |
| Temperature, ℃ | 349 | 461 | 197 |
| Pressure, bar (a) | 1.806 | 1.9 | 1.7 |
| Molar flow rate, kmol/hr | 233.22 | 11.10 | 1868.12 |
| Mass flow rate, kg/hr | 83,000 | 4,981 | 72,019 |
| Massfraction, % | |||
| H2 | 0.0000 | 0.0000 | 0.0070 |
| H2S | 0.0000 | 0.0000 | 0.0110 |
| CH4 | 0.0000 | 0.0000 | 0.0170 |
| CO2 | 0.0000 | 0.0000 | 0.0010 |
| C2H4 | 0.0000 | 0.0000 | 0.1029 |
| C2H6 | 0.0000 | 0.0000 | 0.0090 |
| C3H6 | 0.0001 | 0.0000 | 0.3216 |
| C3H8 | 0.0000 | 0.0000 | 0.0190 |
| i-C4H8 | 0.0001 | 0.0000 | 0.0779 |
| C4H10 | 0.0001 | 0.0000 | 0.0779 |
| 1-C4H8 | 0.0000 | 0.0000 | 0.0549 |
| H20 | 0.0001 | 0.0000 | 0.0669 |
| 32℃ | 0.0001 | 0.0000 | 0.0260 |
| 58℃ | 0.0000 | 0.0000 | 0.0060 |
| 73℃ | 0.0000 | 0.0000 | 0.0060 |
| 86℃ | 0.0001 | 0.0000 | 0.0060 |
| 100℃ | 0.0001 | 0.0000 | 0.0060 |
| 114℃ | 0.0001 | 0.0000 | 0.0080 |
| 128℃ | 0.0001 | 0.0000 | 0.0080 |
| 142℃ | 0.0001 | 0.0000 | 0.0090 |
| 156℃ | 0.0001 | 0.0000 | 0.0090 |
| 170℃ | 0.0001 | 0.0000 | 0.0100 |
| 184℃ | 0.0002 | 0.0000 | 0.0130 |
| 198℃ | 0.0003 | 0.0000 | 0.0190 |
| 212℃ | 0.0004 | 0.0000 | 0.0210 |
| 224℃ | 0.0003 | 0.0000 | 0.0120 |
| 239℃ | 0.0002 | 0.0000 | 0.0080 |
| 253℃ | 0.0003 | 0.0000 | 0.0080 |
| 267℃ | 0.0004 | 0.0000 | 0.0080 |
| 281℃ | 0.0005 | 0.0000 | 0.0090 |
| 295℃ | 0.0006 | 0.0000 | 0.0080 |
| 309℃ | 0.0010 | 0.0000 | 0.0090 |
| 322℃ | 0.0010 | 0.0000 | 0.0080 |
| 336℃ | 0.0030 | 0.0000 | 0.0050 |
| 349℃ | 0.0120 | 0.0000 | 0.0040 |
| 366℃ | 0.0690 | 0.0000 | 0.0040 |
| 378℃ | 0.0910 | 0.0000 | 0.0030 |
| 392℃ | 0.0830 | 0.0000 | 0.0010 |
| 406℃ | 0.0860 | 0.0000 | 0.0000 |
| 420℃ | 0.0860 | 0.0000 | 0.0000 |
| 442℃ | 0.1790 | 0.0020 | 0.0000 |
| 469℃ | 0.1680 | 0.0070 | 0.0000 |
| 496℃ | 0.1680 | 0.1845 | 0.0000 |
| 523℃ | 0.0490 | 0.6989 | 0.0000 |
| ＞547℃ | 0.0000 | 0.1073 | 0.0000 |
| SUM | 1.0000 | 1.0000 | 1.0000 |
Table 4
| The logistics title | 114 | 115 | 116 | 117 | 110 |
| Temperature of reaction, ℃ | 73.1 | 112.4 | 19.3 | 374.6 | 30 |
| Reaction pressure, bar (A) | 13.139 | 13.361 | 5 | 13.5 | 1.7 |
| Molar flow, kmol/hr | 82.001 | 58.976 | 1394.75 | 67.599 | 236.656 |
| Mass flow rate, kg/hr | 4500 | 4400 | 45005.3 | 13963.5 | 4263.43 |
| Mass percent, % | |||||
| H2 | 0 | 0 | 0.011 | 0 | 0 |
| H2S | 0 | 0 | 0.018 | 0 | 0 |
| CH4 | 0 | 0 | 0.027 | 0 | 0 |
| CO2 | 0 | 0 | 0.002 | 0 | 0 |
| C2H4 | 0 | 0 | 0.165 | 0 | 0 |
| C2H6 | 0 | 0 | 0.014 | 0 | 0 |
| C3H6 | 0.093 | 0 | 0.506 | 0 | 0 |
| C3H8 | 0.01 | 0 | 0.029 | 0 | 0 |
| i-C4H8 | 0.351 | 0.086 | 0.081 | 0 | 0 |
| C4H10 | 0.322 | 0.18 | 0.075 | 0 | 0 |
| 1-C4H8 | 0.223 | 0.142 | 0.053 | 0 | 0 |
| H2O | 0 | 0 | 0.012 | 0 | 1 |
| PC40℃ | 0 | 0.125 | 0.005 | 0 | 0 |
| PC58℃ | 0 | 0.06 | 0.001 | 0 | 0 |
| PC72℃ | 0 | 0.048 | 0.001 | 0.001 | 0 |
| PC86℃ | 0 | 0.051 | 0 | 0.001 | 0 |
| PC100℃ | 0 | 0.051 | 0 | 0.003 | 0 |
| PC114℃ | 0 | 0.052 | 0 | 0.007 | 0 |
| PC128℃ | 0 | 0.044 | 0 | 0.013 | 0 |
| PC142℃ | 0 | 0.031 | 0 | 0.021 | 0 |
| PC156℃ | 0 | 0.017 | 0 | 0.025 | 0 |
| PC170℃ | 0 | 0.01 | 0 | 0.03 | 0 |
| PC184℃ | 0 | 0.008 | 0 | 0.042 | 0 |
| PC198℃ | 0 | 0.01 | 0 | 0.069 | 0 |
| PC211℃ | 0 | 0.005 | 0 | 0.038 | 0 |
| PC225℃ | 0 | 0.004 | 0 | 0.033 | 0 |
| PC239℃ | 0 | 0.004 | 0 | 0.035 | 0 |
| PC253℃ | 0 | 0.004 | 0 | 0.036 | 0 |
| PC267℃ | 0 | 0.004 | 0 | 0.042 | 0 |
| PC281℃ | 0 | 0.004 | 0 | 0.039 | 0 |
| PC295℃ | 0 | 0.004 | 0 | 0.039 | 0 |
| PC308℃ | 0 | 0.003 | 0 | 0.032 | 0 |
| PC319℃ | 0 | 0.001 | 0 | 0.011 | 0 |
| PC338℃ | 0 | 0.015 | 0 | 0.143 | 0 |
| PC351℃ | 0 | 0.018 | 0 | 0.175 | 0 |
| PC364℃ | 0 | 0.008 | 0 | 0.078 | 0 |
| PC378℃ | 0 | 0.004 | 0 | 0.037 | 0 |
| PC392℃ | 0 | 0.002 | 0 | 0.021 | 0 |
| PC406℃ | 0 | 0.001 | 0 | 0.014 | 0 |
| PC420℃ | 0 | 0.001 | 0 | 0.007 | 0 |
| PC440℃ | 0 | 0.001 | 0 | 0.007 | 0 |
| PC467℃ | 0 | 0 | 0 | 0.001 | 0 |
| PC497℃ | 0 | 0 | 0 | 0 | 0 |
| PC522℃ | 0 | 0 | 0 | 0 | 0 |
| PC554℃ | 0 | 0 | 0 | 0 | 0 |
| PC574℃ | 0 | 0 | 0 | 0 | 0 |
| Add up to | 1.000 | 1.000 | 1.000 | 1.000 | 1.000 |
Claims (14)
1, a kind of separation method of hydrocarbon oil catalytic cracking reaction products, it is characterized in that this method may further comprise the steps: (a) reaction oil gas (101) of the cracking reactor of autocatalysis is in the future introduced the cold bottom of presorting tower (1) of changing, and inject catalytic pyrolysis raw material (102) by this top of tower, the catalytic pyrolysis raw material in the process that flows downward with mobile reaction oil gas counter current contact upwards and be heated; Reaction oil gas stream temperature in the process of flowing that makes progress constantly reduces, heavy constituent wherein and the catalyst dust of being carried secretly enter the tower bottom branch and draw with slurry oil at the bottom of the tower (104), the catalytic pyrolysis raw material is drawn through side line (103), and light oil distillate and remaining gas stream (105) are extracted out from cat head; (b) from cold change to presort to send into the triphase separator (3) after logistics (105) cooling that column overhead extracts out separate; After boosting, the compressed machine of the gaseous stream that obtains after the separation (108) delivers to follow-up gas separation unit, the condensed liquid (111) that phlegma that obtains after the separation (109) and gaseous stream (108) produce after compression converges to be sent into rectifying tower (2) for logistics (131) and separates, and the sewage that obtains after the separation (110) send Sewage treatment systems.
2,, it is characterized in that described logistics (131) is separated into gaseous stream (113) based on the following cut of C3, the logistics (114) based on C3, C 4 fraction, gasoline fraction (115) in rectifying tower and based on the tower base stream (117) of heavy petrol and diesel oil distillate according to the method for claim 1; Wherein, (113) deliver to follow-up gas separation unit, send into follow-up C3, C4 separation system based on the logistics (114) of C3, C 4 fraction, and gasoline fraction (115) is sent into aromatic hydrocarbons extracting unit, and tower base stream (117) returns the catalytic cracking reaction device.
3, according to the method for claim 1, it is characterized in that described cold changing presort tower and be followed successively by tower still, cooling washing section and heat exchange fractionation zone from bottom to top, the height of tower still accounts for this cold 5-20% that presorts the tower total height that changes, the height of cooling washing section accounts for this cold 10-40% that presorts the tower total height that changes, and the height of heat exchange fractionation zone accounts for this cold 40-80% that presorts the tower total height that changes.
4,, it is characterized in that described catalytic pyrolysis raw material of drawing through side line (103) sends into directly that cat-cracker reacts or send into cat-cracker again and react behind shortening according to the method for claim 1.
5, according to the method for claim 1, it is characterized in that described cold changing presort tower one or more mid-pumparound is set, promptly from cold change the middle and lower part of presorting tower from side line extract out one liquid (106) after cooling off from extracting out mouthful above or extracting out mouthful following or return in the tower by the extraction mouth.
6, according to the method for claim 1, it is characterized in that the described cold working pressure of presorting tower that changes is 0.1-0.35Mpa, service temperature is cat head 100-280 ℃, at the bottom of the tower 350-500 ℃.
7, according to the method for claim 6, it is characterized in that the described cold working pressure of presorting tower that changes is 0.15-0.25MPa, service temperature is cat head 120-250 ℃, at the bottom of the tower 380-480 ℃.
8, according to the method for claim 1, it is characterized in that described cold changing presort the tower side line to extract the temperature of logistics (103) out be 300-400 ℃, the temperature that logistics (106) is extracted in mid-pumparound out is 300-450 ℃, and the temperature of return logistics (107) is 120-280 ℃.
9, according to the method for claim 8, it is characterized in that described cold changing presort the tower side line to extract the temperature of logistics (103) out be 320-380 ℃, the temperature that logistics (106) is extracted in mid-pumparound out is 350-420 ℃, and the temperature of return logistics (107) is 150-250 ℃.
10, according to the method for claim 1, it is characterized in that described cold changing presort in the tower reaction oil gas to go into the tower temperature be 500-800 ℃, 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 described cold changing presort in the tower reaction oil gas to go into the tower temperature be 550-700 ℃, it is 50-100 ℃ that heavy oil feedstock is gone into the tower temperature.
12, according to the method for claim 1 or 2, the working pressure that it is characterized in that described rectifying tower is 0.5-1.6MPA, its cat head service temperature is 10-60 ℃, it is 30-120 ℃ that first side-stream (114) is extracted temperature out, it is 80-300 ℃ that second side line (115) is extracted temperature out, and service temperature is 200-450 ℃ at the bottom of the tower.
13, according to the method for claim 12, the cat head service temperature that it is characterized in that described rectifying tower is 20-50 ℃, it is 50-90 ℃ that first side-stream (114) is extracted temperature out, and it is 100-200 ℃ that second side line (115) is extracted temperature out, and service temperature is 250-400 ℃ at the bottom of the tower.
14,, it is characterized in that described cooled mid-pumparound returns in the tower below extracting out mouthful according to the method for claim 5.
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