CN210560276U - Device for comprehensively utilizing styrene heavy distillate oil - Google Patents
Device for comprehensively utilizing styrene heavy distillate oil Download PDFInfo
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- CN210560276U CN210560276U CN201921655140.7U CN201921655140U CN210560276U CN 210560276 U CN210560276 U CN 210560276U CN 201921655140 U CN201921655140 U CN 201921655140U CN 210560276 U CN210560276 U CN 210560276U
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Abstract
The utility model belongs to the technical field of styrene tar is retrieved and is recycled, a device that utilizes is carried out to styrene heavy distillate oil comprehensively is related to. The device comprises a styrene device rectifying tower, a styrene heavy fraction oil storage tank, a riser reactor and a catalytic cracking device fractionating tower, wherein the bottom of the styrene device rectifying tower is communicated with the styrene heavy fraction oil storage tank through a heavy fraction pipeline at the bottom of the styrene device rectifying tower, the styrene heavy fraction oil storage tank is communicated with the riser reactor through a cross line, and the top of the riser reactor is communicated with the catalytic cracking device fractionating tower through an outlet oil-gas pipeline of the riser reactor. The device provided by the utility model does not need to carry out great under the condition that changes that moves to each apparatus for producing, turns into products such as catalytic gasoline, diesel oil and liquefied gas of high value with styrene heavy distillate oil, improves its economic utilization and worth.
Description
Technical Field
The utility model belongs to the technical field of styrene tar is retrieved and is recycled, a device that utilizes is carried out to styrene heavy distillate oil comprehensively is related to.
Background
The production process of styrene product mainly includes two-stage process, firstly, benzene and ethylene are undergone the process of catalytic reaction to produce ethylbenzene, then the ethylbenzene is undergone the process of catalytic dehydrogenation reaction to produce styrene, in the course of product rectification partial heavy fraction can be produced, also called styrene tar, its yield is about 2% -5% of styrene product quantity. The heavy fraction oil has complicated components, consists of styrene, dimeric styrene, alkylbenzene, diphenyl isopropane, diphenylethylene, polycyclic aromatic hydrocarbon, small amount of polymerization inhibitor and other components, and is easy to produce polymerization reaction and form gel or solid at low temperature.
The conventional treatment method of the produced styrene heavy distillate oil by petrochemical enterprises is to burn the heavy distillate oil as fuel of a heating furnace or to further process the heavy distillate oil for downstream enterprises after leaving factories. If heavy distillate oil is fed into a heating furnace to be used as fuel for combustion, the content of nitrogen oxides in the flue gas discharged by the heating furnace is easy to exceed the standard, the increasingly strict environmental protection index requirements are not met, and the problems of frequent coking and blockage of a burner are easy to occur; if the heavy distillate oil leaves the factory, the styrene heavy distillate oil is listed into hazardous waste along with the new edition of national hazardous waste entry (2016), qualified units must be entrusted to treat the hazardous waste, certain treatment cost is required, and the factory treatment of the styrene heavy distillate oil is limited. Thus, petrochemical enterprises need a device to treat styrene heavy distillate more environmentally and economically.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a device that utilizes multipurposely is carried out styrene heavy distillate oil, under the condition that does not need to carry out great movement to each apparatus for producing and change, turn into products such as catalytic gasoline, diesel oil and liquefied gas of high value with styrene heavy distillate oil, improve its economic utilization value, avoided simultaneously leaving the factory as dangerous waste material with styrene heavy distillate oil or as the fuel of heating furnace results in the nitrogen oxide content in the flue gas to exceed the problem emergence that the environmental protection index required.
In order to achieve the purpose, the utility model is realized by adopting the following technical scheme:
the utility model provides a pair of carry out comprehensive utilization's device to styrene heavy fraction oil, including styrene device rectifying column, styrene heavy fraction oil storage tank, riser reactor and catalytic cracking unit fractionating tower, styrene device rectifying column bottom is linked together through styrene device rectifying column tower bottom heavy fraction pipeline and styrene heavy fraction oil storage tank, and styrene heavy fraction oil storage tank is linked together through the cross-line and riser reactor, and riser reactor top is linked together through riser reactor export oil gas pipeline and catalytic cracking unit fractionating tower.
Further, the crossover is in communication with a catalyst-contacting reaction zone at the middle or bottom of the riser reactor.
Furthermore, 4 groups of spray heads are arranged at the interface of the overline connection riser reactor.
Further, the lowest nominal pressure of the spray head is 5.0 MPa.
Further, a flow control valve is arranged on the crossover line.
Furthermore, a feeding control valve is arranged on a feeding pipeline of the riser reactor at the bottom of the riser reactor, and the feeding control valve and the flow control valve are electrically connected with the controller.
Further, the lowest nominal pressure of the flow control valve is 5.0 MPa.
Furthermore, the pipeline between the cross-line flow control valve and the riser reactor is made of stainless steel, and the pipeline between the flow control valve and the outlet pipeline of the styrene heavy fraction oil storage tank is made of carbon steel.
During operation, the storage temperature of the styrene heavy distillate oil storage tank is optimized and adjusted, the styrene heavy distillate oil is conveyed to a catalyst contact reaction section at the middle part or the bottom part of a riser reactor of the catalytic cracking device through a pipeline, the operation parameters such as the feeding proportion of the heavy distillate oil, the reaction temperature and the pressure of the riser are controlled within a proper range, the styrene heavy distillate oil is contacted with the catalyst of the catalytic cracking device and a series of reactions occur, most of the styrene heavy distillate oil is converted into high-value products such as catalytic gasoline, diesel oil and liquefied gas, and meanwhile, a small amount of dry gas and coke are produced as byproducts, so that the aim of processing and utilizing the styrene heavy distillate oil with.
Adopt above-mentioned technical scheme, the beneficial effects of the utility model are that:
(1) the device of the utility model relies on the existing processing flow of petrochemical enterprises, and takes the heavy fraction oil of styrene as the feeding of the riser reactor of the catalytic cracking device under the condition of not needing to greatly modify each production device, thereby realizing the purpose of utilizing the heavy fraction oil of styrene in high value and environmental protection processing;
(2) the styrene heavy distillate oil is contacted with a high-temperature catalytic cracking catalyst and reacts, more than 85% of the generated products are high-value liquid products such as catalytic gasoline, diesel oil, liquefied gas and the like, and a small amount of dry gas and coke are remained, so that the economic utilization value of the products is improved;
(3) the styrene heavy distillate oil is not used as the fuel of the heating furnace to burn, so that the problem that the content of nitrogen oxides in the discharged flue gas cannot meet the requirement of environmental protection indexes due to the fact that the heating furnace burns the styrene heavy distillate oil is avoided;
(4) the styrene heavy distillate oil is not taken as hazardous waste to leave a factory any more, and the consignment and disposal cost of the hazardous waste is not generated;
and (3) benefit analysis:
the specific benefit is calculated as follows:
when the heavy fraction oil of styrene is used as fuel for burning a heating furnace, the price is about 2000 yuan/ton; when the heavy styrene distillate oil is subjected to catalytic reaction, more than 85% of the heavy styrene distillate oil is converted into liquid products such as catalytic gasoline, diesel oil, liquefied gas and the like, the price is about 7200 yuan/ton, the rest 15% of the heavy styrene distillate oil is dry gas, coke and the like, the price is about 2000 yuan/ton, and the total price of the reaction products of the heavy styrene distillate oil is 85%. 7200+ 15%. 2000. 6420 yuan/ton. Therefore, compared with the price of the heavy styrene distillate oil used as the fuel of a heating furnace, the price of the heavy styrene distillate oil after catalytic reaction is increased by 6420-2000 yuan/ton to 4420 yuan/ton.
Taking a styrene plant of 8.5 ten thousand tons/year scale as an example, the heavy fraction oil yield is calculated as 3% of the styrene product yield, and 2550 tons of styrene heavy fraction oil are produced each year. The catalytic reaction of the heavy fraction of styrene can increase the benefit of 2550X 4420-1127.10 ten thousand yuan per year compared with the catalytic reaction of the heavy fraction of styrene as the fuel of a heating furnace.
Considering that the processing cost such as energy consumed when a catalytic device processes styrene heavy fraction oil is 80 yuan/ton, the processing cost needs to be increased by 80 × 2550 to 20.4 ten thousand yuan each year.
After the process cost is deducted, the economic benefit can be produced as 1127.10-20.4-1106.7 ten thousand yuan/year.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention.
In the drawings:
FIG. 1 is a schematic flow chart of example 1;
FIG. 2 is a schematic flow chart of comparative example 1;
the respective symbols in the figure are as follows: the system comprises a 1 styrene device rectifying tower, a 2 styrene product pipeline, a 3 styrene device rectifying tower bottom heavy fraction pipeline, a 4 styrene heavy fraction oil storage tank, a 5 styrene heavy fraction oil delivery pipeline, a 6 riser reactor, a 7 riser reactor feeding pipeline, an 8 riser reactor outlet oil gas pipeline, a 9 catalytic cracking device fractionating tower, a 10 catalytic cracking device liquid product pipeline, a 11 catalytic cracking device dry gas product pipeline, a 12 riser reactor stripping section, a 13 crossover line and a 14 flow control valve.
Detailed Description
In the description of the present invention, it should be noted that the terms "vertical", "upper", "lower", "horizontal", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
The present invention will be further explained with reference to the accompanying drawings.
The main equipment is as follows: the riser reactor of the catalytic cracking device is an MIP-CGP series riser reactor, and the catalytic cracking raw material is hydrogenated wax oil.
As shown in fig. 1, the bottom of a styrene device rectifying tower 1 is communicated with a styrene heavy fraction oil storage tank 4 through a heavy fraction pipeline 3 at the bottom of the styrene device rectifying tower, the styrene heavy fraction oil storage tank is communicated with a riser reactor 6 through a crossover 13, and the top of the riser reactor is communicated with a catalytic cracking device fractionating tower 9 through an outlet oil-gas pipeline 8 of the riser reactor.
Four groups of stainless steel nozzles are arranged at the interface of the cross-line connection riser reactor. The lowest nominal pressure of the spray head is 5.0 MPa.
The top product of the styrene device rectifying tower is sent out of the styrene device rectifying tower through a styrene product pipeline 2, the bottom product is sent to a styrene heavy distillate oil storage tank for storage through a heavy distillate oil pipeline at the bottom of the styrene device rectifying tower, and the stored heavy distillate oil is periodically sent to a loading system through a heavy distillate oil delivery pipeline 5 to leave a factory or be used as fuel for burning in a heating furnace.
The raw material of the catalytic cracking device enters a feeding atomization section at the bottom of the riser reactor through a feeding pipeline 7 of the riser reactor, the raw material of the catalytic cracking device contacts with a catalyst in the riser reactor and generates a series of reactions, oil gas generated by the reactions enters a fractionating tower of the catalytic cracking device through an outlet oil gas pipeline at the top end of the riser reactor for further separation, separated liquid products such as catalytic liquefied gas, catalytic gasoline and catalytic diesel oil are sent out of the device through a liquid product pipeline 10 of the catalytic cracking device, and separated dry gas products are sent out of the device through a dry gas product pipeline 11 of the catalytic cracking device at the top of the device. Coke products of the catalytic cracking unit in the stripping section 12 of the riser reactor are attached to the surface of the catalyst and enter a regeneration system together with the catalyst for coking.
Meanwhile, a styrene heavy distillate oil storage tank is added to the cross line of the catalytic cracking unit riser reactor, the styrene heavy distillate oil is introduced into a catalyst contact reaction section at the middle part or the bottom part of the catalytic cracking unit riser reactor, and a flow control valve 14 is arranged on the cross line. And a mass flowmeter is arranged on the overline. The flow control valve and the feeding pipeline control valve at the bottom of the riser are set to be in linkage control. Flow control valves controlling the transfer of material across the line are common in the art.
The lowest nominal pressure of the flow control valve is 5.0 MPa.
The material of the flow control valve is carbon steel. The pipeline between the cross-line flow control valve and the riser reactor is made of stainless steel, and the pipeline between the flow control valve and the outlet pipeline of the styrene heavy distillate oil storage tank is made of carbon steel.
In order to avoid repetition, the raw materials and preparation condition parameters related to this specific embodiment are described below in a unified manner, and are not described in detail in the specific embodiment:
the heavy fraction oil of styrene is the heavy fraction produced by rectification in the technical process of generating ethylbenzene by the catalytic reaction of benzene and ethylene and generating styrene by the catalytic dehydrogenation reaction of ethylbenzene. The styrene heavy distillate oil has the property that the density is 900kg/m at 20 DEG C3-1100kg/m3The aromatic hydrocarbon content is 90-100%, and the viscosity at 20 ℃ is 8.0mm2/s-12.0mm2/s。
The catalyst comprises a molecular sieve, a substrate and a binder, wherein the compound components in the catalyst comprise alumina, silica, rare earth elements and phosphorus, wherein the content of alumina in the fresh catalyst which is not regenerated is more than or equal to 42 percent, the content of silica is more than or equal to 40 percent, the micro-activity index is more than or equal to 67 percent, and the specific surface area is more than or equal to 180m2The pore volume is more than or equal to 0.30 ml/g. The catalyst employed in the following examples was a HCGP-2 catalytic cracking catalyst.
The micro-activity index of the equilibrium catalyst contacted with the styrene heavy distillate oil in the riser reactor is controlled to be 52-65 and the specific surface area is more than or equal to 110m by adjusting the replacement rate of adding the fresh catalyst into the reverse regeneration system of the catalytic cracking device2The pore volume is more than or equal to 0.28 ml/g.
(1) Adjusting the storage temperature of a styrene heavy distillate oil storage tank to 75-120 ℃;
(2) the heavy styrene distillate oil is controlled by a flow control valve to enter a riser reactor through a cross line, and in the riser reactor, the heavy styrene distillate oil is mixed with the raw material of a catalytic cracking device, wherein the amount of the heavy styrene distillate oil accounts for 0.8-5% of the total weight proportion of the feeding material of the riser; contacting and reacting with a catalyst in a riser reactor; the outlet temperature of the riser reactor is 490-535 ℃, and the pressure is 150-350 kPa; the main reactions of the styrene heavy distillate oil under the action of the catalyst comprise that side chains of aromatic hydrocarbon are cracked and converted into low-carbon olefin and aromatic hydrocarbon with smaller side chains, and the side chains of the low-carbon olefin and the aromatic hydrocarbon are subjected to transalkylation and dehydrogenation condensation reactions and converted into polycyclic aromatic hydrocarbon, coke and the like;
(3) the oil gas generated by the catalytic reaction of the heavy styrene distillate oil and the reaction oil gas of the raw material of the catalytic device enter a fractionating tower together for subsequent separation.
Example 1
In this example, the raw material of the catalytic cracking unit was hydrogenated wax oil, and when 4t/h of styrene heavy distillate oil was sent to the riser of the catalytic cracking unit for recycle (accounting for 0.98% of the catalytic raw material), the yield of the product was calculated by the amount of the raw material of the catalytic cracking unit (not containing heavy distillate oil), and the yield of the catalytic liquid product was 91.15%, and the yield of the dry gas and coke product was 9.83%. The main operating parameters and product properties are shown in table 1.
TABLE 1 comprehensive utilization of heavy styrene distillate oil, main operating parameters and product properties
Example 2
In this example, the process flow was the same as in example 1. The main difference between this example and example 1 is that the flow of styrene heavy fraction oil to the catalytic recycle and part of the operating parameters were adjusted.
When 7t/h of styrene heavy distillate oil is sent to a catalytic cracking device and a riser is recycled (accounting for 1.71 percent of the catalytic raw material), the product yield is calculated according to the amount of the catalytic raw material (without the heavy distillate oil), the yield of catalytic liquid products is 91.77 percent, and the yield of dry gas and coke products is 9.94 percent. The main operating parameters and product properties are shown in table 2.
TABLE 2 comprehensive utilization of heavy fraction oil of styrene, main operating parameters and product properties
Comparative example 1
Unlike example 1, as shown in fig. 2, the cross line 13 from the styrene heavy fraction oil storage tank to the riser reactor of the catalytic cracking unit is eliminated, and the styrene heavy fraction oil does not enter the riser reactor to perform the catalytic reaction.
When the catalytic cracking unit does not recycle the styrene heavy distillate, the product yield is calculated according to the amount of the catalytic raw material, the yield of the obtained catalytic liquid product is 90.3%, and the yield of the dry gas and coke products is 9.7%. The main operating parameters and product properties are shown in table 3.
TABLE 3 Main operating parameters and product Properties for catalytic cracking of catalytic cracker feed
Example 1 compared to comparative example 1, when 4t/h of styrene heavy distillate oil was sent to the catalytic cracker riser for recycle, the yield of catalytic liquid product increased by 0.85 percentage point, which corresponds to an increase of 3.47t/h, and the yield of dry gas and coke product increased by 0.13 percentage point, which corresponds to an increase of 0.53 t/h. The calculation shows that 86.8 percent of the heavy styrene distillate oil is converted into liquid products such as catalytic liquefied gas, gasoline, diesel oil and the like after catalytic cracking reaction, and 13.2 percent of the heavy styrene distillate oil is converted into catalytic dry gas and coke products.
Example 2 compared to comparative example 1, when 7t/h of styrene heavy distillate oil is sent to the riser of the catalytic cracking unit for recycling, the yield of catalytic liquid products is improved by 1.47 percentage points, which is equivalent to 6.02t/h increase, and the yield of dry gas and coke products is improved by 0.24 percentage points, which is equivalent to 0.98t/h increase. The calculation shows that 86.0% of the heavy styrene distillate oil is converted into liquid products such as catalytic liquefied gas, gasoline, diesel oil and the like after catalytic cracking reaction, and 14.0% of the heavy styrene distillate oil is converted into catalytic dry gas and coke products.
As can be seen from the data shown in Table 1, Table 2 and Table 3, when the heavy styrene distillate oil is sent to the riser of the catalytic cracking device for recycling, 86.4% of the heavy styrene distillate oil is averagely converted into liquid products such as catalytic liquefied gas, gasoline and diesel oil, and 13.6% of the heavy styrene distillate oil is converted into catalytic dry gas and coke products. Compared with the technology of the comparative example 1, the problem that the content of nitrogen oxides in the flue gas exceeds the requirement of environmental protection indexes because the heavy styrene distillate oil is taken as hazardous waste to leave a factory or is taken as fuel of a heating furnace is avoided, and meanwhile, the comprehensive utilization value of the heavy styrene distillate oil is improved.
And (3) benefit calculation:
(1) when the heavy fraction oil of styrene is sent to a riser of a catalytic cracking device for recycling, 86.4 percent of the heavy fraction oil of styrene is converted into liquid products such as catalytic liquefied gas, gasoline, diesel oil and the like, the price of the heavy fraction oil of styrene is about 7200 yuan/ton, and 13.6 percent of the heavy fraction oil of styrene is converted into catalytic dry gas and coke products, and the price of the heavy fraction oil of styrene is about 2000 yuan/ton. The overall price of the reaction product of the heavy styrene distillate is calculated to be 86.4% 7200+ 13.6% 2000-6492.8 yuan/ton, which is increased by 6492.8-2000-4492.8 yuan/ton compared with the price of the reaction product as the fuel of the heating furnace. Taking a styrene plant of 8.5 ten thousand tons/year scale as an example, about 2550 tons of heavy styrene distillate oil can be produced each year, and the increased benefit is 2550 × 4492.8 ═ 1145.66 ten thousand yuan.
(2) Taking a styrene plant of 8.5 ten thousand tons/year scale as an example, considering that the processing cost such as energy consumed when a catalytic cracker processes styrene heavy fraction oil is 80 yuan/ton, it is necessary to increase the processing cost 2550 × 80 to 20.4 ten thousand yuan per year.
After the process cost is deducted, the economic benefit can be produced as 1145.66-20.4-1125.26 ten thousand yuan/year.
It is to be understood that the present invention has been described in detail with reference to the foregoing embodiments, and that modifications and equivalents of the various embodiments described above may be made by those skilled in the art, or some of the technical features may be substituted. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. The device for comprehensively utilizing the styrene heavy distillate oil is characterized by comprising a styrene device rectifying tower (1), a styrene heavy distillate oil storage tank (4), a riser reactor (6) and a catalytic cracking device fractionating tower (9), wherein the bottom of the styrene device rectifying tower (1) is communicated with the styrene heavy distillate oil storage tank (4) through a heavy distillate oil pipeline (3) at the bottom of the styrene device rectifying tower, the styrene heavy distillate oil storage tank (4) is communicated with the riser reactor (6) through a cross line (13), and the top of the riser reactor (6) is communicated with the catalytic cracking device fractionating tower (9) through an outlet oil-gas pipeline (8) of the riser reactor.
2. The apparatus for comprehensive utilization of styrene heavy distillate oil according to claim 1, wherein said crossover (13) is in communication with a catalyst-contacting reaction zone at the middle or bottom of the riser reactor (6).
3. The apparatus for comprehensive utilization of styrene heavy distillate oil according to claim 1, wherein 4 groups of nozzles are disposed at the interface of the crossover line (13) connected to the riser reactor (6).
4. The apparatus for the comprehensive utilization of styrene heavy fraction oil according to claim 3, wherein the minimum nominal pressure of said nozzles is 5.0 MPa.
5. The apparatus for the comprehensive utilization of styrene heavy distillate oil according to claim 1, wherein said crossover (13) is provided with a flow control valve (14).
6. The apparatus for comprehensive utilization of styrene heavy distillate oil according to claim 5, wherein the riser reactor feed line (7) at the bottom of the riser reactor (6) is provided with a feed control valve, and the feed control valve and the flow control valve (14) are electrically connected with the controller.
7. Device for the comprehensive utilization of styrene heavy distillate oil according to claim 5, characterized in that the minimum nominal pressure of said flow control valve (14) is 5.0 MPa.
8. The apparatus for comprehensive utilization of styrene heavy fraction oil according to claim 5, wherein the crossover (13) is made of stainless steel in the pipe between the flow control valve (14) and the riser reactor (6), and is made of carbon steel in the pipe between the flow control valve (14) and the outlet pipe of the styrene heavy fraction oil storage tank (4).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110511783A (en) * | 2019-09-30 | 2019-11-29 | 中国石油化工股份有限公司 | The device and method that styrene heavy distillate is comprehensively utilized |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110511783A (en) * | 2019-09-30 | 2019-11-29 | 中国石油化工股份有限公司 | The device and method that styrene heavy distillate is comprehensively utilized |
| CN110511783B (en) * | 2019-09-30 | 2023-09-29 | 中国石油化工股份有限公司 | Device and method for comprehensively utilizing styrene heavy distillate oil |
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