CN106924984B - Method for controlling liquid level and reaction severity of tower bottom of fractionating tower - Google Patents
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 82
- 239000007788 liquid Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 68
- 239000002002 slurry Substances 0.000 claims abstract description 47
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 13
- 239000000571 coke Substances 0.000 claims abstract description 8
- 239000003921 oil Substances 0.000 claims description 131
- 235000019198 oils Nutrition 0.000 claims description 124
- 239000007789 gas Substances 0.000 claims description 13
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 239000010775 animal oil Substances 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000003502 gasoline Substances 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 235000015112 vegetable and seed oil Nutrition 0.000 claims description 4
- 239000008158 vegetable oil Substances 0.000 claims description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 239000010779 crude oil Substances 0.000 claims description 3
- 239000002283 diesel fuel Substances 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 2
- 239000003208 petroleum Substances 0.000 claims description 2
- 239000003079 shale oil Substances 0.000 claims description 2
- 239000011275 tar sand Substances 0.000 claims description 2
- 230000003197 catalytic effect Effects 0.000 claims 1
- 238000005194 fractionation Methods 0.000 claims 1
- 150000002431 hydrogen Chemical class 0.000 claims 1
- 238000010924 continuous production Methods 0.000 abstract description 2
- 239000003054 catalyst Substances 0.000 description 42
- 239000007787 solid Substances 0.000 description 12
- 208000012839 conversion disease Diseases 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 239000010724 circulating oil Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- GZGREZWGCWVAEE-UHFFFAOYSA-N chloro-dimethyl-octadecylsilane Chemical compound CCCCCCCCCCCCCCCCCC[Si](C)(C)Cl GZGREZWGCWVAEE-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4283—Bottom stream
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A method for controlling the liquid level at the bottom of fractionating tower and the reaction severity. The method comprises the following steps: the herringbone plate of the fractionating tower is positioned at the lower part of the fractionating tower, a catalytic cracking raw oil medium subjected to heat exchange is introduced at a position near the vertical height of the herringbone plate on the side wall of the fractionating tower, wherein the mass ratio of the catalytic cracking raw oil medium to a catalytic cracking reaction product entering the fractionating tower is 1: 1000-0.5: 1; the position near the vertical height of the herringbone plate on the side wall of the fractionating tower is the side wall of the fractionating tower between the herringbone plate and the inlet position of the catalytic cracking reaction product or the side wall of the fractionating tower between the herringbone plate and the outlet position of the return oil slurry. The method of the invention controls the liquid level at the bottom of the fractionating tower and the reaction severity, effectively reduces the yield of the catalytic cracking coke and realizes the continuous production of the device.
Description
Technical Field
The present invention relates to a control method in a catalytic cracking process.
Background
Catalytic cracking is one of the most important heavy oil upgrading processes. The catalytic cracking process has the advantages of low investment, low operation cost, strong raw material adaptability, high yield of light products and mature technology, and is the main source of profits of the current oil refineries (Zulihua. the current development situation and the prospect of the catalytic cracking technology in China [ J ]. petrochemical engineering technology economy, 2000, 16 (1): 16-21.). At present, the annual processing capacity of catalytic cracking in China exceeds 1 hundred million t, and in the composition of commercial gasoline, the catalytic cracking gasoline accounts for about 80 percent, the diesel oil accounts for about 30 percent, and more than 30 percent of propylene comes from the catalytic cracking process.
The fractionating tower is one of the important processes of the catalytic cracking unit. Factors affecting the liquid level at the bottom of the fractionating tower include reaction temperature, change of solvent-oil ratio, change of reaction time, change of refining oil amount, change of oil slurry recycling amount, change of oil slurry returning amount, change of temperature at the bottom of the fractionating tower, change of oil slurry external throwing amount and the like (Wu Ruizang, coke coming, Pang Qing Min, Cao just, improvement of the scheme for controlling the liquid level at the bottom of the fractionating tower of the small catalytic cracking unit [ J ] petrochemical automation, 2002 (5): 50-51.). Generally, the liquid level at the bottom of a fractionating tower of a catalytic cracking unit is controlled to be about 30-40%. However, with the increase of the demand of catalytic cracking units for light oil at home and abroad, a plurality of units are modified into MIP or MIP-CGP, or the severity of the units is increased, or a high-activity catalyst is selected, and then the liquid level at the bottom of a catalytic cracking fractionating tower is difficult to maintain.
Wu Lai Zheng et al "improvement of control scheme for liquid level at bottom of fractionating tower in small catalytic cracking unit" points out the factors affecting liquid level at bottom of fractionating tower, such as reaction temperature variation, oil refining amount variation, oil slurry returning amount and temperature variation, and oil slurry external throwing amount variation.
With the development of high-severity catalytic cracking processes (MIP, MGD, CPP, DCC and the like) and catalysts (HBO, HDO, CDOS and the like), the liquid level at the bottom of a fractionating tower is difficult to control, the coking at the bottom of the fractionating tower is influenced, and the coking at the bottom of the fractionating tower becomes one of important factors influencing the long period of a catalytic cracking device. Most of the technologies do not introduce external raw materials to control the tower bottom coking of the fractionating tower by controlling the liquid level of the tower bottom of the fractionating tower, and cannot fundamentally solve the density and solid content of the tower bottom slurry of the fractionating tower.
In conclusion, when the liquid level of the oil slurry at the bottom of the fractionating tower rises, the adjustment can be carried out by means of improving the reaction severity, increasing the external throwing amount and the like, but the solid content and the density of the oil slurry at the bottom of the fractionating tower can be increased, and the risk of coking at the bottom of the fractionating tower is increased; when the liquid level of the bottom oil slurry of the fractionating tower is reduced, the adjustment can be carried out by means of reducing the reaction severity, reducing the external throwing amount and the like, but the yield of the target product is inevitably reduced, so that the economic benefit of the device is reduced.
Disclosure of Invention
The invention aims to provide a method for controlling the liquid level at the bottom of a fractionating tower and the reaction severity, which can effectively reduce the coke yield of catalytic cracking reaction products and has equivalent liquid yield.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower, wherein a herringbone plate of the fractionating tower is positioned at the lower part of the fractionating tower, and the method comprises the following steps: introducing a catalytic cracking raw oil medium subjected to heat exchange at a position near the vertical height of a herringbone plate on the side wall of the fractionating tower, wherein the mass ratio of the catalytic cracking raw oil medium to a catalytic cracking reaction product entering the fractionating tower is 1: 1000-0.5: 1; the position near the vertical height of the herringbone plate on the side wall of the fractionating tower is the side wall of the fractionating tower between the herringbone plate and the inlet position of the catalytic cracking reaction product or the side wall of the fractionating tower between the herringbone plate and the outlet position of the return oil slurry.
The invention discloses a method for controlling the tower bottom liquid level and the reaction severity of a fractionating tower, wherein the mass ratio of a medium to reaction oil gas is 1: 1000-0.5: 1, preferably 1: 500-0.5: 1, and more preferably, the liquid level height H of the introduced catalytic cracking raw oil medium subjected to heat exchange is selectedSupplement deviceSatisfies the relation HSupplement device＝H1-H2In which H is1The value of (A) is 28 to 50, more preferably 30 to 48; h2×∏×D2123- (0.5 to 2) × C × 100, preferably H2×∏×D 22 ÷ 4 × ρ ═ 123- (0.6 to 1.5) × C × 100; wherein C is the catalytic cracking conversion rate, the inner diameter of the fractionating tower is D, and the density of the bottom oil slurry of the fractionating tower is rho.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower, wherein the inner diameter of the fractionating tower and the density of slurry at the tower bottom of the fractionating tower are common knowledge in the field.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower, wherein the liquid level height of introduced catalytic cracking raw oil medium subjected to heat exchange refers to a percentage value of a variation numerical value of the liquid level vertical height after the catalytic cracking raw oil medium subjected to heat exchange is introduced into the fractionating tower relative to the vertical distance from the tower bottom of the fractionating tower to the lower part of a herringbone plate, and the mathematical expression is as follows: hSupplement deviceThe change value of the liquid level vertical height after the catalytic cracking raw oil medium subjected to heat exchange is introduced is 100/the vertical distance from the bottom of the fractionating tower to the lower part of the herringbone plate.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower.
The invention discloses a method for controlling the liquid level at the bottom of a fractionating tower and the reaction severity, wherein the catalytic cracking conversion rate can visually express the conversion depth, and is the sum of the yields of dry gas, liquefied gas, gasoline and coke in a catalytic cracking reaction product.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower, wherein the catalytic cracking raw oil medium after heat exchange is 100-380 ℃, preferably 150-350 ℃.
The invention discloses a method for controlling the liquid level and the reaction severity of the bottom of a fractionating tower, which is a separation device connected between a riser oil gas outlet and an absorption stabilizing tower and is well known to a person skilled in the art.
The invention discloses a method for controlling the liquid level and the reaction severity of the tower bottom of a fractionating tower.
The present invention discloses a method for controlling the liquid level at the bottom of a fractionating tower and the reaction severity, wherein the catalytic cracking raw oil medium is well known to those skilled in the art. The catalytic cracking raw oil medium can be natural hydrocarbon oil with the boiling point of not less than 300 ℃ and synthetic hydrocarbon-containing oil. The catalytic cracking raw oil medium can also have a density of 0.85-1.20 g.cm at 20 DEG C-3Natural and synthetic hydrocarbon-containing oils. Based on 100 parts of the mass composition of the catalytic cracking raw oil, 90-80 parts of carbon element and 10-20 parts of hydrogen element, preferably 88-85 parts of carbon element and 12-15 parts of hydrogen element. The common catalytic cracking raw oil is selected from one or more of vacuum wax oil, normal pressure wax oil, poor diesel oil, various animal and vegetable oils rich in hydrocarbon, vacuum residual oil, raffinate oil, deasphalted oil, coking wax oil, shale oil, tar sand oil and heavy residual petroleum crude oil.
The various animal and vegetable oils rich in hydrocarbon can be one or more of animal oil, vegetable oil and synthetic oil.
The invention discloses a method for controlling the liquid level at the bottom of a fractionating tower and the reaction severity, wherein the material trend of a reaction oil gas product in the fractionating tower is as follows: the reaction oil gas enters the bottom of a fractionating tower after heat exchange, the light component is distilled to obtain the light component after passing through a herringbone plate, the oil slurry is pumped out and exchanges heat through a circulating oil slurry pump, part of the tower bottom oil slurry enters a lifting pipe as the return oil slurry, part of the oil slurry is pumped out by an external throwing oil slurry pump, and part of the oil slurry returns to the upper part and the lower part of the herringbone plate as a cooling medium and a cleaning medium; the catalytic cracking raw oil medium subjected to heat exchange is introduced from a position near the vertical height of the herringbone plate on the side wall of the fractionating tower, and the position near the vertical height of the herringbone plate on the side wall of the fractionating tower is the side wall of the fractionating tower between the herringbone plate and the reaction oil gas inlet position or the side wall of the fractionating tower between the herringbone plate and the return oil outlet position.
According to the method for controlling the liquid level and the reaction severity of the tower bottom of the fractionating tower, the catalytic cracking raw oil medium is introduced into the fractionating tower, the amount of liquid can be supplemented according to the liquid level of the tower bottom of the fractionating tower, and meanwhile, the density and the solid content of the bottom oil slurry of the fractionating tower can be effectively adjusted due to the fact that the added catalytic cracking raw oil medium is light in density and does not carry catalyst powder, and by the method, the liquid level of the tower bottom of the fractionating tower does not need to consider the reaction severity of catalytic cracking and the activity change of a catalyst, the coke yield of a catalytic cracking device is low, and therefore continuous production of the device can be achieved; meanwhile, the liquid yield of the catalytic cracking is equivalent to that of the prior art. On the other hand, the catalytic cracking raw oil medium is introduced into the method disclosed by the invention, so that part of heat at the lower part of the fractionating tower can be absorbed, the energy consumption of the device is reduced, and the fractionating efficiency of the fractionating tower is improved.
Drawings
In the figure 1, a raw oil medium enters a fractionating tower through the upper part of a herringbone plate, wherein 1-a fractionating tower, 2-an external throwing oil slurry outlet, 3-a catalytic cracking reaction product inlet, 4-the herringbone plate, 5-a raw oil medium inlet, 6-a refined oil slurry outlet, 7-an oil slurry upward return tower inlet and 8-an oil slurry downward return tower inlet.
FIG. 2 is a diagram of raw oil medium entering a fractionating tower through the lower part of a herringbone plate, wherein 1-a fractionating tower, 2-an external throwing oil slurry outlet, 3-a catalytic cracking reaction product inlet, 4-the herringbone plate, 5-a raw oil medium inlet, 6-a refined oil slurry outlet, 7-an oil slurry upward returning tower inlet and 8-an oil slurry downward returning tower inlet.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments. The drawings and detailed description do not limit the scope of the invention as claimed.
In the drawings of the figure 1 and the figure 2, raw oil medium enters a fractionating tower through the upper part and the lower part of a herringbone plate, wherein 1-the fractionating tower, 2-an external throwing oil slurry outlet, 3-a catalytic cracking reaction product inlet, 4-the herringbone plate, 5-a raw oil medium inlet, 6-a refined oil slurry outlet, 7-an oil slurry upward-returning tower inlet and 8-an oil slurry downward-returning tower inlet.
Main raw materials and sources
HDO-70 fresh catalyst and HDC-200 catalyst, produced by catalyst works of the Lanzhou petrochemical company.
The raw oil is taken from raw oil of a 300 ten thousand ton/year catalytic cracking device of Lanzhou petrochemical company (properties are shown in table 1), the raw oil is hereinafter referred to as 300 ten thousand catalyst, and the mass ratio of the vacuum wax oil to the vacuum residue oil is (6: 4).
TABLE 1 Properties of the feed oils
The reaction oil gas enters the bottom of the fractionating tower after heat exchange, the light component is distilled to obtain the light component after passing through the herringbone plate, the oil slurry is pumped out by a circulating oil slurry pump and exchanges heat, a part of the oil slurry enters a lifting pipe as the recycled oil slurry, a part of the oil slurry is pumped out by an external throwing oil slurry pump, and a part of the oil slurry respectively enters the upper part and the lower part of the herringbone plate and returns to the fractionating tower; the catalytic cracking raw oil medium subjected to heat exchange is introduced from a position near the vertical height of the herringbone plate on the side wall of the fractionating tower, and the position near the vertical height of the herringbone plate on the side wall of the fractionating tower is the side wall of the fractionating tower between the herringbone plate and the reaction oil gas inlet position or the side wall of the fractionating tower between the herringbone plate and the return oil outlet position.
Example 1
Referring to fig. 1, 300 million catalyst is in contact reaction with a regenerated catalyst in a 300 million ton/year catalytic cracking unit in Lanzhou, the catalyst is HDO-70 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions of 500 ℃ of reaction temperature, 6 of catalyst-oil ratio and 1.9s of reaction time; specific reaction conditions and results are shown in table 2. The medium is decompression wax oil, and the mass ratio of the flow of the raw oil medium entering the fractionating tower to the reaction oil gas is 1: 20. The reaction conversion rate is 74.26 percent, and the oil slurry density is 1.01g/cm3The liquid level at the bottom of the fractionating column was 35.
Example 2
Referring to FIG. 2, 300 ten thousand catalysts are in contact reaction with a regenerated catalyst in an MIP type catalytic cracking device with the call of 260 ten thousand tons/year, the catalyst is HDC-200 fresh catalyst, and the catalyst oil is prepared at the reaction temperature of 490 DEG CThe reaction mixture enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the condition that the time of the first reaction zone is 1.0 s/3.5 s; specific reaction conditions and results are shown in table 2. The medium is 300 million catalysts, and the mass ratio of the medium entering the fractionating tower to the reaction oil gas 2 is 1: 5. The reaction conversion rate is 72.87 percent, and the oil slurry density is 1.08g/cm3The liquid level at the bottom of the column was 38.
Example 3
Referring to fig. 2, 300 million of catalyst is in contact reaction with a regenerated catalyst in an MIP type catalytic cracking device of 260 million tons/year in the call of Haoshi, the catalyst is HDC-200 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions of reaction temperature of 520 ℃, catalyst-oil ratio of 5.5 and time of 1.0s in a first reaction zone/3.5 s in a second reaction zone; specific reaction conditions and results are shown in table 2. The medium is 300 million catalysts, and the mass ratio of the medium entering the fractionating tower to the reaction oil gas 2 is 1: 13. The reaction conversion rate is 69.17 percent, and the oil slurry density is 1.05g/cm3The liquid level at the bottom of the column was 42.
Example 4
Referring to fig. 2, 300 million of catalyst is in contact reaction with a regenerated catalyst in an MIP type catalytic cracking device of 260 million tons/year in the call of Haoshi, the catalyst is HDO-70 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions that the reaction temperature is 510 ℃, the catalyst-oil ratio is 7.2, and the time of a first reaction zone is 1.0 s/the time of a second reaction zone is 3.5 s; specific reaction conditions and results are shown in table 2. The medium is 300 million catalysts, and the mass ratio of the medium entering the fractionating tower to the reaction oil gas 2 is 1: 32. The reaction conversion rate is 75.97 percent, and the oil slurry density is 1.05g/cm3The liquid level at the bottom of the fractionating column was 45.
Example 5
Referring to fig. 2, 300 million of catalyst is in contact reaction with a regenerated catalyst in an MIP type catalytic cracking device of 260 million tons/year in the call of Haoshi, the catalyst is HDC-200 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions of reaction temperature of 515 ℃, catalyst-oil ratio of 8.1 and time of 1.0s in a first reaction zone/3.5 s in a second reaction zone; specific reaction conditions and results are shown in table 2. The medium is 300 million catalyst, and the medium enters the flow of the fractionating towerThe mass ratio of the reaction oil gas to the reaction oil gas 2 is 1: 100. The reaction conversion rate is 83.37 percent, and the oil slurry density is 1.05g/cm3The liquid level at the bottom of the column was 46.
Example 6
Referring to fig. 2, 300 million of catalyst is in contact reaction with a regenerated catalyst in a 100 million tons/year MIP type catalytic cracking device in Daqing petrochemical industry, the catalyst is HDO-70 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions of 500 ℃ of reaction temperature, 6.5 of catalyst-oil ratio and 1.0s of time of a first reaction zone/3.5 s of time of a second reaction zone; specific reaction conditions and results are shown in table 2. The medium is 300 million catalysts, and the mass ratio of the medium entering the fractionating tower to the reaction oil gas 2 is 1: 55. The reaction conversion rate is 78.57 percent, and the oil slurry density is 1.05g/cm3The liquid level at the bottom of the fractionating column was 40.
Comparative example 1
Referring to fig. 2, 300 million of catalyst is in contact reaction with a regenerated catalyst in a 100 million tons/year MIP type catalytic cracking device in Daqing petrochemical industry, the catalyst is HDC-200 fresh catalyst, and enters a gas-solid settling separator and the bottom of a fractionating tower 1 after reaction under the conditions of 500 ℃ of reaction temperature, 8.1 of catalyst-oil ratio and 1.0s of time of a first reaction zone/3.5 s of time of a second reaction zone; specific reaction conditions and results are shown in table 2. The medium was not introduced into the column and the liquid level at the bottom of the column was 25.
As can be seen from table 2, in comparative example 1, when the catalytic cracking is at high reaction severity, the yield of heavy oil is low, so the liquid level at the bottom of the fractionating tower is also low, and the solid content and density of heavy oil are also high, so that coke is particularly easily generated at the bottom of the fractionating tower, which affects the long-term operation of the apparatus, while in examples 1 to 6, by adopting the method of the present invention, the catalytic cracking raw oil medium is added into the fractionating tower, the density and solid content of heavy oil are significantly reduced, the product yield is improved, the coke selectivity is significantly reduced, and the total liquid yield is equivalent.
TABLE 2 reaction conditions and reaction results
Claims (8)
1. A method for controlling the liquid level and reaction severity in the bottom of a fractionation column having a chevron plate located in the lower portion of the column, comprising: introducing a catalytic cracking raw oil medium subjected to heat exchange at a position near the vertical height of a herringbone plate on the side wall of the fractionating tower, wherein the mass ratio of the catalytic cracking raw oil medium to a catalytic cracking reaction product entering the fractionating tower is 1: 1000-0.5: 1; the position near the vertical height of the herringbone plate on the side wall of the fractionating tower is the side wall of the fractionating tower between the herringbone plate and the inlet position of the catalytic cracking reaction product, or the side wall of the fractionating tower between the herringbone plate and the outlet position of the return oil slurry; the temperature of the catalytic cracking raw oil medium subjected to heat exchange is 100-380 ℃.
2. The method according to claim 1, wherein the mass ratio of the catalytic cracking raw oil medium to the catalytic cracking reaction product entering the fractionating tower is 1: 500-0.5: 1.
3. The method of claim 1, wherein the catalytic cracking conversion is the sum of yields of dry gas, liquefied gas, gasoline, and coke in the catalytic cracking reaction product.
4. The method according to claim 1 or 2, wherein the temperature of the heat-exchanged catalytic cracked stock oil medium is 150-350 ℃.
5. The method according to claim 1 or 2, wherein the catalytically cracked feedstock medium is a natural hydrocarbon oil/synthetic hydrocarbon-containing oil having a boiling point of not less than 300 ℃, or has a density of 0.85 to 1.20g.cm at 20 ℃-3Natural/synthetic hydrocarbon-containing oils.
6. The method according to claim 1 or 2, wherein the catalytically cracked stock oil medium comprises 90 to 80 parts by mass of carbon element and 10 to 20 parts by mass of hydrogen element, based on 100 parts by mass of the catalytically cracked stock oil medium.
7. The method according to claim 6, wherein the catalytically cracked stock oil medium comprises 88 to 85 parts by mass of carbon and 12 to 15 parts by mass of hydrogen, based on 100 parts by mass of the catalytically cracked stock oil medium.
8. The method according to claim 5, wherein the catalytically cracked crude oil medium is selected from one or more of vacuum wax oil, atmospheric wax oil, low-grade diesel oil, various hydrocarbon-rich animal and vegetable oils, vacuum residuum, raffinate oil, deasphalted oil, coker wax oil, shale oil, tar sand oil, and heavy residual petroleum crude oil.
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| CN203768311U (en) * | 2014-01-26 | 2014-08-13 | 中石化洛阳工程有限公司 | Delayed coking device |
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| CN106924984A (en) | 2017-07-07 |
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