CN114149827A - Gasoline processing flow for reducing silicon content - Google Patents
Gasoline processing flow for reducing silicon content Download PDFInfo
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- CN114149827A CN114149827A CN202111580777.6A CN202111580777A CN114149827A CN 114149827 A CN114149827 A CN 114149827A CN 202111580777 A CN202111580777 A CN 202111580777A CN 114149827 A CN114149827 A CN 114149827A
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- point components
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- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 229910052710 silicon Inorganic materials 0.000 title claims abstract description 60
- 239000010703 silicon Substances 0.000 title claims abstract description 60
- 239000002994 raw material Substances 0.000 claims abstract description 43
- CZDYPVPMEAXLPK-UHFFFAOYSA-N tetramethylsilane Chemical compound C[Si](C)(C)C CZDYPVPMEAXLPK-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000010992 reflux Methods 0.000 claims abstract description 19
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000009835 boiling Methods 0.000 claims description 13
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000002156 mixing Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
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Classifications
-
- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A gasoline processing flow for reducing silicon content relates to the technical field of gasoline processing, and comprises the following steps: s1, taking raw material gasoline; s2, heating the raw material gasoline by a heat exchanger, and introducing the heated raw material gasoline into a fractionating tower for fractionating, wherein the tower inlet temperature is 45-65 ℃; s3, enabling the temperature of the top of the fractionating tower to be 40-50 ℃, enabling the pressure to be 0.08-0.09 MPa, enabling low-boiling-point components containing a large amount of tetramethylsilane to flow out of the top of the fractionating tower, cooling to 15-25 ℃, collecting in a reflux tank, enabling a part of low-boiling-point components to flow back to the fractionating tower and a part of low-boiling-point components to be sent to a riser of a catalytic cracking device; s4, controlling the temperature of the bottom of the fractionating tower to be 110-120 ℃, enabling high-boiling-point components containing a small amount of tetramethylsilane to flow out of the bottom of the fractionating tower, enabling a part of the high-boiling-point components to be reboiled by a reboiler and then return to the fractionating tower, and enabling a part of the high-boiling-point components to be cooled by a heat exchanger and then be sent to a gasoline tank area; the gasoline processing flow can be used for pretreating the silicon-containing gasoline, greatly reducing the silicon content in the gasoline and reducing the recycling amount of the silicon-containing gasoline.
Description
Technical Field
The invention relates to the technical field of gasoline processing, in particular to a gasoline processing flow for reducing silicon content.
Background
With the continuous upgrade of national gasoline standards, the environmental protection technical requirement of gasoline for vehicles JingVIB, which is implemented at 12.1.12.1.2021, increases the index of silicon content no more than 2ppm, and in the production process of the gasoline in the traditional refinery, the problem that the silicon content of the gasoline product exceeds the standard due to factors such as the recycling of the silicon-containing dirty oil, the addition of a silicon-containing agent and the like exists; the main component of silicon in the gasoline is tetramethylsilane, the gasoline containing silicon is generally recycled in a riser of a catalytic cracking device, and the silicon in the gasoline is removed through the adsorption action of a catalyst; in actual production, after a large amount of silicon-containing finished gasoline is processed by a catalytic cracking unit, the processing load of the catalytic cracking unit is occupied, and repeated processing of a large amount of product gasoline is caused, so that the normal production of a refinery is influenced, the stock of the refinery is occupied, and the economic benefit loss of the refinery is caused; therefore, the adoption of a more optimized processing flow, the reduction of the silicon content in the gasoline and the reduction of the remill quantity of the silicon-containing gasoline are key problems to be solved.
Disclosure of Invention
In order to overcome the defects in the background art, the invention discloses a gasoline processing flow for reducing silicon content, which can be used for pretreating silicon-containing gasoline, greatly reducing the silicon content in the gasoline and reducing the remilling quantity of the silicon-containing gasoline.
In order to achieve the purpose, the invention adopts the following technical scheme:
a gasoline processing flow for reducing silicon content comprises the following steps: s1, taking raw material gasoline, wherein the content of tetramethylsilane is 10-30 ppm; s2, heating the raw material gasoline by a heat exchanger, and introducing the heated raw material gasoline into a fractionating tower for fractionating, wherein the tower inlet temperature is 45-65 ℃; s3, enabling the temperature of the top of the fractionating tower to be 40-50 ℃, enabling the pressure to be 0.08-0.09 MPa, enabling low-boiling-point components containing a large amount of tetramethylsilane to flow out of the top of the fractionating tower, cooling to 15-25 ℃, collecting in a reflux tank, enabling a part of low-boiling-point components to flow back to the fractionating tower, sending a part of low-boiling-point components to a riser of a catalytic cracking device, and sending the low-boiling-point components to a gasoline tank area after catalytic cracking; s4, the temperature of the bottom of the fractionating tower is 110-120 ℃, high-boiling-point components containing a small amount of tetramethylsilane flow out from the bottom of the fractionating tower, a part of the high-boiling-point components is boiled again by a reboiler and then returns to the fractionating tower, and a part of the high-boiling-point components is cooled by a heat exchanger and then is sent to a gasoline tank area.
Further, in the step S1, the raw gasoline is taken out through a raw material buffer tank, and the temperature in the raw material buffer tank is 15 to 25 ℃.
Further, in step S3, the low boiling point component is cooled by passing through an air cooler and an overhead circulating water cooler in this order.
Further, in the step S3, the reflux ratio of the low boiling point component is 1 to 2.
Further, in step S4, the high boiling point components are cooled to 15-25 ℃ by a bottom circulating water cooler before being sent to the gasoline tank zone.
Furthermore, the fractionating tower has 50 layers of tower plates, and the feed inlet of the raw material gasoline is 22 layers of tower plates.
Further, in the step S3, the yield of the low-boiling-point component is 15-20%, and the content of tetramethylsilane is 100-200 ppm.
Further, in the step S4, the yield of the high-boiling-point component is 80 to 85%, and the content of tetramethylsilane is 2ppm or less.
Due to the adoption of the technical scheme, the invention has the following beneficial effects:
the gasoline processing flow for reducing the silicon content disclosed by the invention utilizes the characteristic that the boiling point of tetramethylsilane is lower, adopts the processing flow of fractionation to cut the silicon-containing gasoline lightly and heavily, so that the tetramethylsilane is enriched in a small amount of low-boiling-point components, the low-boiling-point components enter a riser of a catalytic cracking device, the tetramethylsilane in the low-boiling-point gasoline components is removed by utilizing the adsorption capacity of a catalyst, and a large amount of high-boiling-point gasoline components with the silicon content not more than 2ppm can be directly fed into a gasoline tank area to serve as gasoline blending components; compared with the traditional gasoline processing flow, the proportion of the silicon-containing gasoline recycled by the riser of the catalytic cracking device is reduced by 80-85%, the occupation of the load of the catalytic cracking device and the influence on the normal production of a refinery are greatly reduced, meanwhile, the processing flow is simple, the operation cost is low, and the benefit of the refinery can be effectively improved.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention.
Detailed Description
In the following description, the technical solutions of the present invention will be described with reference to the drawings of the embodiments of the present invention, and it should be understood that, if there is an orientation or positional relationship indicated by terms such as "upper", "lower", "front", "rear", "left", "right", etc., it is only corresponding to the drawings of the present invention, and for convenience of describing the present invention, it is not necessary to indicate or imply that the indicated devices or elements have a specific orientation:
the gasoline processing flow for reducing the silicon content in combination with the attached figure 1 comprises the following steps:
taking raw material gasoline, wherein the content of tetramethylsilane is 10-30 ppm; according to the requirements, raw gasoline is taken from a raw material buffer tank, the temperature in the raw material buffer tank is 15-25 ℃, tetramethylsilane is prevented from being vaporized due to the boiling point of tetramethylsilane under the standard condition of 26.5 ℃, and the raw gasoline in the raw material buffer tank is pumped out through a raw material pump;
step two, heating the raw material gasoline by a heat exchanger, and introducing the heated raw material gasoline into a fractionating tower for fractionating, wherein the fractionating tower is provided with 50 layers of tower plates, a feed inlet of the raw material gasoline is provided with 22 layers of tower plates, and the tower inlet temperature is 45-65 ℃;
step three, the temperature of the top of the fractionating tower is 40-50 ℃, the pressure is 0.08-0.09 MPa, tetramethylsilane is enriched on the top of the fractionating tower after being vaporized, and low-boiling-point components containing a large amount of tetramethylsilane flow out of the top of the fractionating tower, are cooled to 15-25 ℃ and are collected in a reflux tank; according to the requirement, the low-boiling-point components are cooled sequentially through the air cooler and the tower top circulating water cooler, so that the cooling efficiency is improved; the yield of the low-boiling-point components is 15-20%, the content of tetramethylsilane is 100-200 ppm, part of the low-boiling-point components in the reflux tank flow back to the fractionating tower through a reflux pump, the reflux ratio is 1-2, and one part of the low-boiling-point components is sent to a riser of a catalytic cracking device and sent to a gasoline tank area after catalytic cracking;
fourthly, the temperature of the bottom of the fractionating tower is 110-120 ℃, a small amount of high-boiling-point components containing tetramethylsilane flow out from the bottom of the fractionating tower, the yield of the high-boiling-point components is 80-85%, the content of tetramethylsilane is below 2ppm, a part of the high-boiling-point components is reboiled by a reboiler and then returns to the fractionating tower, and a part of the high-boiling-point components is conveyed by a bottom pump, cooled by a heat exchanger and then sent to a gasoline tank area; and (3) cooling the high-boiling-point components to 15-25 ℃ by a circulating water cooler at the bottom of the tower before the high-boiling-point components are delivered to the gasoline tank area according to requirements.
The invention is illustrated in further detail by the following examples:
the first embodiment is as follows:
the silicon content of the raw material silicon-containing gasoline is 17.74ppm, the flow rate is 79.4t/h, the raw material silicon-containing gasoline firstly passes through a raw material buffer tank and a raw material pump, then is heated to 49 ℃ through a heat exchanger and enters a gasoline fractionating tower, the temperature at the top of the tower is 46 ℃, the pressure at the top of the tower is 0.095MPa, the low boiling point component at the top of the tower is cooled to 19 ℃ through an air cooler and a circulating water cooler and then enters a return tank at the top of the tower, then passes through a return pump at the top of the tower, the silicon content of the gasoline is conveyed out of the top of the tower to 113.3ppm, the conveying amount is 12.6t/h, the gasoline is conveyed to a riser of a downstream catalytic cracking device, and the other part of the gasoline is returned to the tower as reflux, wherein the reflux ratio is 1.3; and (3) returning a high-boiling-point component to the tower after one part of the tower bottom is reboiled by a tower bottom reboiler, wherein the temperature of the tower bottom is 114 ℃, and the other part of the high-boiling-point component is cooled to 21 ℃ by a tower bottom pump through a heat exchanger and a tower bottom circulating water cooler, and then sending the high-boiling-point component serving as a tower bottom gasoline product to a tank field for blending, wherein the delivery amount is 66.8t/h, and the silicon content is 0.57 ppm.
Example two:
the silicon content of the raw material silicon-containing gasoline is 18.85ppm, the flow rate is 81t/h, the raw material silicon-containing gasoline firstly passes through a raw material buffer tank and a raw material pump, then is heated to 49 ℃ through a heat exchanger, enters a gasoline fractionating tower, the temperature at the top of the tower is 48 ℃, the pressure at the top of the tower is 0.085MPa, the low boiling point component at the top of the tower is cooled to 20 ℃ through an air cooler and a circulating water cooler, then enters a tower top return tank, then passes through a tower top return pump, the silicon content of the gasoline is 137.32ppm outside the top of the tower, the delivery amount is 12.7t/h, the gasoline is delivered to a riser of a downstream catalytic cracking device, and the other part of the gasoline is returned to the tower as reflux, wherein the reflux ratio is 1.3; and (3) returning a high-boiling-point component from one part of the tower bottom to the tower after reboiling by a tower bottom reboiler, wherein the temperature of the tower bottom is 113 ℃, and the other part of the high-boiling-point component is cooled to 20 ℃ by a tower bottom pump through a heat exchanger and a tower bottom circulating water cooler, and then sending the high-boiling-point component serving as a tower bottom gasoline product to a tank area for blending, wherein the delivery amount is 68.3t/h, and the silicon content is 0.27 ppm.
Example three:
the silicon content of the raw material silicon-containing gasoline is 25.04ppm, the flow rate is 66t/h, the raw material silicon-containing gasoline firstly passes through a raw material buffer tank and a raw material pump, then is heated to 63 ℃ through a heat exchanger, enters a gasoline fractionating tower, the temperature of the top of the tower is 47 ℃, the pressure of the top of the tower is 0.085MPa, the low boiling point component at the top of the tower is cooled to 21 ℃ through an air cooler and a circulating water cooler, then enters a tower top return tank, then passes through a tower top return pump, the silicon content of the gasoline is 143.12ppm outside the top of the tower, the delivery amount is 11t/h, the gasoline is delivered to a riser of a downstream catalytic cracking device, and the other part of the gasoline is returned to the tower as reflux, wherein the reflux ratio is 1.2; and (3) returning a high-boiling-point component to the tower after one part of the tower bottom is reboiled by a tower bottom reboiler, wherein the temperature of the tower bottom is 114 ℃, and the other part of the high-boiling-point component is cooled to 23 ℃ by a tower bottom pump through a heat exchanger and a tower bottom circulating water cooler, and then sending the high-boiling-point component serving as a tower bottom gasoline product to a tank area for blending, wherein the delivery amount is 55t/h, and the silicon content is 1.03 ppm.
Example four:
the silicon content of the raw material silicon-containing gasoline is 29.48ppm, the flow rate is 72t/h, the raw material silicon-containing gasoline firstly passes through a raw material buffer tank and a raw material pump, then is heated to 61 ℃ through a heat exchanger, enters a gasoline fractionating tower, the temperature at the top of the tower is 48 ℃, the pressure at the top of the tower is 0.085MPa, the low boiling point component at the top of the tower is cooled to 19 ℃ through an air cooler and a circulating water cooler, then enters a tower top return tank, then passes through a tower top return pump, the silicon content of the gasoline is 165.48ppm outside the top of the tower, the delivery amount is 12t/h, the gasoline is delivered to a riser of a downstream catalytic cracking device, and the other part of the gasoline is returned to the tower as reflux with the reflux ratio of 1; and a high-boiling-point component returns to the tower after being reboiled by a reboiler at the bottom of the tower from one part of the tower, the temperature of the tower bottom is 114 ℃, and the other part of the high-boiling-point component is cooled to 21 ℃ by a material inlet and outlet heat exchanger and a circulating water cooler at the bottom of the tower through a pump at the bottom of the tower, and then the high-boiling-point component is taken as a gasoline product at the bottom of the tower and sent to a tank area for blending, wherein the delivery amount is 60t/h, and the silicon content is 3.22 ppm.
Example five:
the silicon content of the raw material silicon-containing gasoline is 23.83ppm, the flow rate is 75t/h, the raw material silicon-containing gasoline firstly passes through a raw material buffer tank and a raw material pump, then is heated to 50 ℃ through a heat exchanger and enters a gasoline fractionating tower, the temperature at the top of the tower is 47 ℃, the pressure at the top of the tower is 0.099MPa, the low boiling point component at the top of the tower is cooled to 25 ℃ through an air cooler and a circulating water cooler and then enters a tower top return tank, then passes through a tower top return pump, the silicon content of the gasoline is 157.68ppm outside the top of the tower, the delivery amount is 10.5t/h, the gasoline is delivered to a riser of a downstream catalytic cracking device, and the other part of the gasoline is returned to the tower as reflux, wherein the reflux ratio is 1.6; and a high-boiling-point component returns to the tower after being reboiled by a reboiler at the bottom of the tower from one part of the tower, the temperature of the tower bottom is 111 ℃, and the other part of the high-boiling-point component is cooled to 25 ℃ by a material inlet and outlet heat exchanger and a circulating water cooler at the bottom of the tower through a pump at the bottom of the tower, and then the high-boiling-point component is taken as a gasoline product at the bottom of the tower and sent to a tank area for blending, wherein the delivery amount is 64.5t/h, and the silicon content is 1.83 ppm.
The invention is not described in detail in the prior art, and it is apparent to a person skilled in the art that the invention is not limited to details of the above-described exemplary embodiments, but that the invention can be embodied in other specific forms without departing from the spirit or essential characteristics thereof; the present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein, and any reference signs in the claims are not intended to be construed as limiting the scope of the claims concerned.
Claims (8)
1. A gasoline processing flow for reducing silicon content is characterized in that: comprises the following steps:
s1, taking raw material gasoline, wherein the content of tetramethylsilane is 10-30 ppm;
s2, heating the raw material gasoline by a heat exchanger, and introducing the heated raw material gasoline into a fractionating tower for fractionating, wherein the tower inlet temperature is 45-65 ℃;
s3, enabling the temperature of the top of the fractionating tower to be 40-50 ℃, enabling the pressure to be 0.08-0.09 MPa, enabling low-boiling-point components containing a large amount of tetramethylsilane to flow out of the top of the fractionating tower, cooling to 15-25 ℃, collecting in a reflux tank, enabling a part of low-boiling-point components to flow back to the fractionating tower, sending a part of low-boiling-point components to a riser of a catalytic cracking device, and sending the low-boiling-point components to a gasoline tank area after catalytic cracking;
s4, the temperature of the bottom of the fractionating tower is 110-120 ℃, high-boiling-point components containing a small amount of tetramethylsilane flow out from the bottom of the fractionating tower, a part of the high-boiling-point components is boiled again by a reboiler and then returns to the fractionating tower, and a part of the high-boiling-point components is cooled by a heat exchanger and then is sent to a gasoline tank area.
2. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in the step S1, raw gasoline is taken through a raw material buffer tank, and the temperature in the raw material buffer tank is 15-25 ℃.
3. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in the step S3, the low boiling point components are cooled by passing through an air cooler and an overhead circulating water cooler in this order.
4. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in the step S3, the reflux ratio of the low boiling point component is 1-2.
5. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in step S4, the high boiling point components are cooled to 15-25 ℃ by a circulating water cooler at the bottom of the tower before being sent to the gasoline tank area.
6. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: the fractionating tower has 50 layers of tower plates, and the feed inlet of the raw material gasoline is 22 layers of tower plates.
7. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in the step S3, the yield of the low-boiling-point component is 15-20%, and the content of tetramethylsilane is 100-200 ppm.
8. The gasoline processing flow for reducing silicon content as claimed in claim 1, wherein: in the step S4, the yield of the high-boiling-point component is 80-85%, and the content of tetramethylsilane is below 2 ppm.
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| CN202111580777.6A CN114149827A (en) | 2021-12-22 | 2021-12-22 | Gasoline processing flow for reducing silicon content |
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| CN202111580777.6A CN114149827A (en) | 2021-12-22 | 2021-12-22 | Gasoline processing flow for reducing silicon content |
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Citations (3)
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|---|---|---|---|---|
| US4176047A (en) * | 1978-04-10 | 1979-11-27 | Continental Oil Company | Removal of organic compounds from coker gasoline |
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2021
- 2021-12-22 CN CN202111580777.6A patent/CN114149827A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4176047A (en) * | 1978-04-10 | 1979-11-27 | Continental Oil Company | Removal of organic compounds from coker gasoline |
| CN107661736A (en) * | 2017-11-09 | 2018-02-06 | 江苏新海石化有限公司 | A kind of double lifting catalytic cracking units and its method for modifying high silicon gasoline inferior |
| CN108444983A (en) * | 2018-03-22 | 2018-08-24 | 山东出入境检验检疫局检验检疫技术中心 | A kind of torch pipe for measuring volatile materials |
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Application publication date: 20220308 |