CN113862020A - Olefin separation device for improving quality of coal-made stable heavy oil - Google Patents
Olefin separation device for improving quality of coal-made stable heavy oil Download PDFInfo
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- CN113862020A CN113862020A CN202010614746.7A CN202010614746A CN113862020A CN 113862020 A CN113862020 A CN 113862020A CN 202010614746 A CN202010614746 A CN 202010614746A CN 113862020 A CN113862020 A CN 113862020A
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- 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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- 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
- C10G2400/20—C2-C4 olefins
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- 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
- C10G2400/22—Higher olefins
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Abstract
本发明涉及一种煤制稳定重质油提质的烯烃分离装置，包括：重油预热器；重油分离塔，重油预热器与重油分离塔的中部连接，重油分离塔设有C11及更轻烃气相出口和C12及更重烃出口；轻烃分离塔，C11及更轻烃气相出口通过轻烃管路与轻烃分离塔的中部连接，轻烃分离塔的设有C5～8混合烃气相出口和C9～11混合烃液相出口，第一真空与轻烃回流罐连接；重烃分离塔，重烃分离塔设有C12～17混合烃气相出口和C19及更重烃液相出口，重烃分离塔设有C12～17混合烃气相出口和C19及更重烃液相出口。本发明的烯烃分离装置能够以煤制稳定重质油为原料，将煤制稳定重质油分离为窄碳数的混合烯烃，有利于简化后续加工过程中的处理难度，市场附加值高。
The invention relates to an olefin separation device for upgrading stable heavy oil made from coal, comprising: a heavy oil preheater; Hydrocarbon gas phase outlet and C12 and heavier hydrocarbon outlet; light hydrocarbon separation tower, C11 and heavier hydrocarbon gas phase outlet is connected to the middle of light hydrocarbon separation tower through light hydrocarbon pipeline, light hydrocarbon separation tower is equipped with C5~8 mixed hydrocarbon gas phase The outlet and the C9-11 mixed hydrocarbon liquid phase outlet, the first vacuum is connected to the light hydrocarbon reflux tank; the heavy hydrocarbon separation tower, the heavy hydrocarbon separation tower is provided with C12-17 mixed hydrocarbon gas phase outlet and C19 and heavier hydrocarbon liquid phase outlet, heavy hydrocarbon separation tower. The hydrocarbon separation tower is provided with a C12-17 mixed hydrocarbon gas phase outlet and a C19 and heavier hydrocarbon liquid phase outlet. The olefin separation device of the invention can use the coal-made stable heavy oil as a raw material, and separate the coal-made stable heavy oil into mixed olefins with narrow carbon number, which is beneficial to simplify the processing difficulty in the subsequent processing process and has high market added value.
Description
Technical Field
The invention relates to the technical field of chemical industry, in particular to an olefin separation device for improving quality of coal-made stable heavy oil.
Background
Alpha-olefin is a very important basic raw material in the petrochemical industry and plays an important role in the petrochemical industry. And the alpha-olefin is used as an important organic raw material and an intermediate product and is widely applied to polyethylene comonomers, surfactants, lubricating oil, plasticizers, poly-alpha-olefin, auxiliaries and fine chemicals. Wherein 1-butene, 1-hexene and 1-octene are mainly used as comonomer of polyethylene, 1-octene and C12 are used as raw material of poly alpha-olefin (PAO), C14-C19 are used for producing detergent, and alpha-olefin with more than C19 is used for producing lubricant and drilling fluid.
The Fischer-Tropsch synthesis coal indirect liquefaction technology is characterized in that CO and H2 in synthesis gas are synthesized into long-carbon-chain hydrocarbon macromolecules through an iron-based catalyst, Fischer-Tropsch synthesis stable heavy oil is one of intermediate products, the stable heavy oil is separated out through a stripping tower, olefins with different carbon chain lengths in the Fischer-Tropsch synthesis heavy oil have long-term significance and wide market prospect, coal-based alpha-olefin has the position that petroleum-based alpha-olefin cannot be replaced, odd-number carbon and high-carbon-number alpha-olefin can be synthesized through a Fischer-Tropsch synthesis process, and the long-carbon-chain hydrocarbon macromolecules can not be obtained industrially through other synthesis processes at present. The carbon number length range of the carbon chain in the Fischer-Tropsch synthesis heavy oil is wide, the conventional treatment mode is hydrogenation to obtain a product with low carbon number, however, olefins with different carbon numbers have different purposes, and the target olefins with narrow carbon number are difficult to obtain.
Disclosure of Invention
The invention provides an olefin separation device capable of obtaining olefins with narrow carbon number and improving the quality of coal-made stable heavy oil with low energy consumption to solve at least one technical problem.
The technical scheme for solving the technical problems is as follows:
an olefin separation device for upgrading coal-made stable heavy oil, comprising:
the heavy oil preheater is used for preheating the coal-made heavy oil;
the discharge port end of the heavy oil preheater is connected with the middle part of the heavy oil separation tower, the heavy oil separation tower is provided with a C11 and lighter hydrocarbon gas phase outlet and a C12 and heavier hydrocarbon outlet, and the top of the heavy oil separation tower is provided with a first vacuum;
the device comprises a light hydrocarbon separation tower, wherein a C11 and lighter hydrocarbon gas-phase outlet is connected with the middle part of the light hydrocarbon separation tower through a light hydrocarbon pipeline, the light hydrocarbon pipeline is sequentially provided with a light hydrocarbon air cooler, a light hydrocarbon water cooler, a light hydrocarbon reflux tank, a light hydrocarbon pump and a light hydrocarbon preheater, the light hydrocarbon separation tower is provided with a C5-8 mixed hydrocarbon gas-phase outlet and a C9-11 mixed hydrocarbon liquid-phase outlet, and the first vacuum is connected with the light hydrocarbon reflux tank;
heavy hydrocarbon knockout tower, heavy hydrocarbon knockout tower is equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and heavier hydrocarbon liquid phase export, C12 and heavier hydrocarbon liquid phase export through the heavy hydrocarbon pipeline with the middle part of heavy hydrocarbon knockout tower is connected, heavy hydrocarbon knockout tower is equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and heavier hydrocarbon liquid phase export, the heavy hydrocarbon knockout tower top is equipped with the second vacuum.
The invention has the beneficial effects that: the olefin separation device can separate the coal-made stable heavy oil into the mixed olefin with narrow carbon number by taking the coal-made stable heavy oil as a raw material, is favorable for simplifying the treatment difficulty in the subsequent processing process, and has high market added value.
On the basis of the technical scheme, the invention can be further improved as follows.
The middle hydrocarbon separation tower is used for separating and obtaining C12-13 mixed hydrocarbons and C14-17 mixed hydrocarbons, a C12-17 mixed hydrocarbon gas phase outlet is connected with the middle of the middle hydrocarbon separation tower through a middle hydrocarbon pipeline, the middle hydrocarbon separation tower is provided with a C12-13 mixed hydrocarbon gas phase outlet and a C14-17 mixed hydrocarbon liquid phase outlet, the C12-13 mixed hydrocarbon gas phase outlet is sequentially connected with a C12-13 mixed hydrocarbon air cooler, a C12-13 mixed hydrocarbon reflux tank and a C12-13 mixed hydrocarbon reflux pump, a third vacuum is arranged at the top of the middle hydrocarbon separation tower, and the third vacuum is connected with the middle hydrocarbon reflux tank.
The beneficial effect of adopting the further scheme is that: the intermediate hydrocarbon separation tower can be used for separating C12-13 mixed hydrocarbons and C14-17 mixed hydrocarbons, so that the separation of olefins with long carbon chain number is facilitated, and the added value of the heavy oil prepared from coal is improved.
Further, an intermediate hydrocarbon air cooler, an intermediate hydrocarbon reflux tank, an intermediate hydrocarbon reflux pump and an intermediate hydrocarbon preheater are sequentially arranged on the intermediate hydrocarbon pipeline, the second vacuum is connected with the intermediate hydrocarbon reflux tank, a C14-17 mixed hydrocarbon liquid phase outlet is connected with a C14-17 mixed hydrocarbon delivery pump, and an outlet end of the C14-17 mixed hydrocarbon delivery pump is connected with a heat source inlet of the intermediate hydrocarbon preheater to serve as a heat source of the intermediate hydrocarbon preheater.
The beneficial effect of adopting the further scheme is that: the method has the advantages that the heat of the C14-17 mixed hydrocarbon in the separation process is used for preheating the feeding material of the middle hydrocarbon separation tower, and the reduction of energy consumption in separation is facilitated.
Further, light hydrocarbon preheater includes first preheater and second preheater, first preheater with the second preheater series connection sets up on the light hydrocarbon pipeline, the heat source export of middle hydrocarbon preheater with the heat source entry linkage of first preheater, C19 and heavier hydrocarbon liquid phase exit linkage have heavy hydrocarbon delivery pump, heavy hydrocarbon delivery pump's exit end with the heat source entry end of second preheater is connected as the heat source of second preheater.
The beneficial effect of adopting the further scheme is that: adopt first pre-heater and second pre-heater, can be through the mode of heat transfer to C19 and heavier hydrocarbon and C14 ~ 17 hydrocarbon mixture further cooling, further reduce the energy consumption.
Further, a light hydrocarbon reboiler is arranged at the bottom of the light hydrocarbon separation tower, a heat source outlet of the light hydrocarbon reboiler is connected with a heat source inlet of the second preheater, and an outlet end of the heavy hydrocarbon delivery pump is connected with a heat source inlet of the light hydrocarbon reboiler.
The beneficial effect of adopting the further scheme is that: the heat source of light hydrocarbon reboiler is connected with the exit end of heavy hydrocarbon delivery pump, and when continuous operation, light hydrocarbon knockout tower need not to provide the heat source again, can further reduce the energy consumption of heavy oil separation.
Further, heavy oil knockout tower, heavy hydrocarbon knockout tower and the bottom of middle hydrocarbon knockout tower all is equipped with the reboiler at the bottom of the tower, the bottom of light hydrocarbon knockout tower is equipped with the reboiler that starts to work, start to work the reboiler with light hydrocarbon reboiler parallel arrangement.
The beneficial effect of adopting the further scheme is that: the light hydrocarbon separation tower is provided with the reboiler of starting work, can provide when starting work and heat the light hydrocarbon, and the reboiler of starting work and light hydrocarbon reboiler establish ties, can switch between the reboiler of starting work and light hydrocarbon reboiler, are favorable to reducing the energy consumption when the light hydrocarbon separates.
Further, the C5-8 mixed hydrocarbon gas phase outlet is sequentially connected with a C5-8 mixed hydrocarbon air cooler, a C5-8 mixed hydrocarbon water cooler, a C5-8 mixed hydrocarbon reflux tank and a C5-8 mixed hydrocarbon reflux pump, and the C9-11 mixed hydrocarbon liquid phase outlet is sequentially connected with a C9-11 mixed hydrocarbon conveying pump, a C9-11 mixed hydrocarbon air cooler and a C9-11 mixed hydrocarbon water cooler.
The beneficial effect of adopting the further scheme is that: 5-8 mixed hydrocarbon products can be cooled through the C5-8 mixed hydrocarbon air coolers, and meanwhile, the C9-11 mixed hydrocarbon air coolers and the C9-11 mixed hydrocarbon water coolers can cool the C9-11 mixed hydrocarbon products.
Further, a heavy oil conveying pipe is arranged at a feeding port of the heavy oil preheater, and a heavy oil olefin coalescer is arranged on the heavy oil conveying pipe.
The beneficial effect of adopting the further scheme is that: the heavy oil olefin coalescer can effectively improve the quality of heavy oil and is beneficial to the separation of olefin.
Further, the light hydrocarbon separating tower still is equipped with the oil wash naphtha conveyer pipe, the oil wash naphtha conveyer pipe passes through the light hydrocarbon preheater with the feed inlet of light hydrocarbon separating tower is connected.
The beneficial effect of adopting the further scheme is that: set up the oil and wash naphtha conveyer pipe, can promote the added value of oil and wash naphtha to the separation of oil and wash naphtha synchronous processing.
Further, an oil-washed naphtha olefin coalescer is arranged on the oil-washed naphtha conveying pipe.
The beneficial effect of adopting the further scheme is that: the oil-washed naphtha olefin coalescer can improve the quality of oil-washed naphtha and is beneficial to olefin separation.
Drawings
FIG. 1 is a block diagram of the preferred embodiment of the present invention.
In the drawings, the components represented by the respective reference numerals are listed below:
1. a heavy oil separation column; 2. a light hydrocarbon separation column; 3. a heavy hydrocarbon separation column; 4. an intermediate hydrocarbon separation column; 5. a heavy oil preheater; 6. a first vacuum; 7. a light hydrocarbon pipeline; 8. a light hydrocarbon air cooler; 9. a light hydrocarbon water cooler; 10. a light hydrocarbon reflux tank; 11. a light hydrocarbon reflux pump; 12. a light hydrocarbon preheater; 121. a first preheater; 122. a second preheater; 13. a heavy hydrocarbon pipeline; 14. a second vacuum; 15. an intermediate hydrocarbon line; 16. c12-13 hydrocarbon mixture air cooler; 17. c12-13 mixed hydrocarbon reflux tank; 18. a C12-13 mixed hydrocarbon reflux pump; 19. a third vacuum; 20. an intermediate hydrocarbon air cooler; 21. an intermediate hydrocarbon reflux drum; 22. an intermediate hydrocarbon reflux pump; 23. an intermediate hydrocarbon preheater; 24. a C14-17 mixed hydrocarbon delivery pump; 25. a heavy hydrocarbon transfer pump; 26. a light hydrocarbon reboiler; 27. a column bottom reboiler; 28. a reboiler is started; 29. c5-8 mixed hydrocarbon air cooler; 30. c5-8 mixed hydrocarbon water cooler; 31. c5-8 mixed hydrocarbon reflux tank; 32. a C5-8 mixed hydrocarbon reflux pump; 33. c9-11 mixed hydrocarbon delivery pump; 34. c9-11 mixed hydrocarbon air cooler; 35. c9-11 mixed hydrocarbon water cooler; 36. a heavy oil delivery pipe; 37. a heavy oil olefin coalescer; 38. an oil-washed naphtha delivery pipe; 39. an oil washed naphtha olefins coalescer.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
Examples
As shown in figure 1, the core of the invention is to provide an olefin separation device for upgrading coal-made stable heavy oil, which comprises: a heavy oil preheater 5 for preheating the coal-made heavy oil, wherein the preheating temperature is 210 ℃; the heavy oil separation tower 1 is characterized in that the discharge port end of a heavy oil preheater 5 is connected with the middle part of the heavy oil separation tower 1, the heavy oil separation tower 1 is provided with a C11 and lighter hydrocarbon gas phase outlet and a C12 and heavier hydrocarbon outlet, and the top of the heavy oil separation tower 1 is provided with a first vacuum 6; the heavy oil separation tower comprises a light hydrocarbon separation tower 2, a C11 and lighter hydrocarbon gas phase outlet and a first vacuum 6, wherein the light hydrocarbon separation tower 2 is connected with the middle part of the light hydrocarbon separation tower 2 through a light hydrocarbon pipeline 7, the light hydrocarbon pipeline 7 is sequentially provided with a light hydrocarbon air cooler 8, a light hydrocarbon water cooler 9, a light hydrocarbon reflux tank 10, a light hydrocarbon reflux pump 11 and a light hydrocarbon preheater 12, the light hydrocarbon reflux pump 11 refluxes a part of light hydrocarbons passing through the light hydrocarbon air cooler 8 and the light hydrocarbon water cooler 9 to the top of a heavy oil separation tower 1 and conveys the part of the light hydrocarbons to the light hydrocarbon separation tower 2, the light hydrocarbon separation tower 2 is provided with a C5-8 mixed hydrocarbon gas phase outlet and a C9-11 mixed hydrocarbon liquid phase outlet, and the first vacuum 6 is connected with the light hydrocarbon reflux tank 10; heavy hydrocarbon knockout tower 3, heavy hydrocarbon knockout tower 3 is equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and more heavy hydrocarbon liquid phase export, C12 and more heavy hydrocarbon liquid phase export are connected through the middle part of heavy hydrocarbon pipeline 13 with heavy hydrocarbon knockout tower 3, heavy hydrocarbon knockout tower 3 is equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and more heavy hydrocarbon liquid phase export, 3 tops of heavy hydrocarbon knockout tower are equipped with second vacuum 14.
Preferably, the device further comprises an intermediate hydrocarbon separation tower 4 for separating and obtaining C12-13 mixed hydrocarbons and C14-17 mixed hydrocarbons, wherein a C12-17 mixed hydrocarbon gas phase outlet is connected with the middle of the intermediate hydrocarbon separation tower 4 through an intermediate hydrocarbon pipeline 15, the intermediate hydrocarbon separation tower 4 is provided with a C12-13 mixed hydrocarbon gas phase outlet and a C14-17 mixed hydrocarbon liquid phase outlet, a C12-13 mixed hydrocarbon gas phase outlet is sequentially connected with a C12-13 mixed hydrocarbon air cooler 16, a C12-13 mixed hydrocarbon reflux tank 17 and a C12-13 mixed hydrocarbon reflux pump 18, a third vacuum 19 is arranged at the top of the intermediate hydrocarbon separation tower 4, the third vacuum 19 is connected with an intermediate hydrocarbon reflux tank 21, the gas-phase C12-13 mixed hydrocarbons are cooled to 60 ℃ through the C12-13 mixed hydrocarbon air cooler 16 and are conveyed to a storage tank for finish machining, and the liquid-phase C14-17 mixed hydrocarbons are subjected to heat exchange and are cooled to 60 ℃ and conveyed to the storage tank for finish machining.
In this embodiment, the vacuum degree at the top of the heavy oil separation tower 1 is-29 kPa, the feeding temperature is 210 ℃, the operating temperature at the top of the heavy oil separation tower 1 is 159 ℃, the operating temperature at the bottom of the heavy oil separation tower is 262 ℃, C11 and lighter hydrocarbons are obtained at the top of the tower, and C12 and heavier hydrocarbons are obtained at the bottom of the tower; the light hydrocarbon separation tower 2 is operated at normal pressure, the pressure at the top of the tower is 8kPa, the feeding temperature is 147 ℃, the operating temperature at the top of the light hydrocarbon separation tower 2 is 113 ℃, C5-8 mixed hydrocarbon is obtained at the top of the tower, and C9-11 mixed hydrocarbon is obtained at the bottom of the tower; the vacuum degree of the top of the heavy hydrocarbon separation tower 3 is-64 kPa, the feeding operation temperature of the heavy hydrocarbon separation tower 3 is 168 ℃, C12-17 mixed hydrocarbon is obtained at the top of the tower, the operation temperature is 232 ℃, C19 and heavier hydrocarbon is obtained at the bottom of the tower, and the operation temperature of the bottom of the tower is 299 ℃; the vacuum degree of the top of the intermediate hydrocarbon separation tower 4 is-58 kPa, the feeding temperature is 205 ℃, the operating temperature of the top of the tower is 183 ℃, the operating temperature of the bottom of the tower is 248 ℃, C12-13 mixed hydrocarbon is obtained at the top of the tower, and C14-17 mixed hydrocarbon is obtained at the bottom of the tower.
Preferably, the intermediate hydrocarbon pipeline 15 is sequentially provided with an intermediate hydrocarbon air cooler 20, an intermediate hydrocarbon reflux tank 21, an intermediate hydrocarbon reflux pump 22 and an intermediate hydrocarbon preheater 23, the second vacuum 14 is connected with the intermediate hydrocarbon reflux tank 21, the liquid phase outlets of the C14-17 mixed hydrocarbons are connected with a C14-17 mixed hydrocarbon delivery pump 24, and the outlet ends of the C14-17 mixed hydrocarbon delivery pump 24 are connected with the heat source inlet of the intermediate hydrocarbon preheater 23 to serve as the heat source of the intermediate hydrocarbon preheater 23.
Preferably, light hydrocarbon preheater 12 includes first preheater 121 and second preheater 122, first preheater 121 and second preheater 122 series connection set up on light hydrocarbon pipeline 7, the heat source export of intermediate hydrocarbon preheater 23 and the heat source entry linkage of first preheater 121, C19 and heavier hydrocarbon liquid phase exit linkage have heavy hydrocarbon delivery pump 25, the exit end of heavy hydrocarbon delivery pump 25 is connected as the heat source of second preheater 122 with the heat source entry end of second preheater 122, the heat source export at first preheater 121 is equipped with C14 ~ 17 mixed hydrocarbon air cooler, cool C14 ~ 17 mixed hydrocarbon to 60 ℃, and carry to the storage tank storage for use.
Preferably, light hydrocarbon knockout tower 2's bottom is equipped with light hydrocarbon reboiler 26, light hydrocarbon reboiler 26's heat source export and the heat source entry linkage of second preheater 122, heavy hydrocarbon transfer pump 25's exit end and light hydrocarbon reboiler 26's heat source entry linkage, be equipped with C19 and heavier hydrocarbon air cooler in the heat source export of second preheater 122, cool C19 and heavier hydrocarbon to 167 ℃, and carry to the hydrofining unit hydrogenation, or with C19 and heavier hydrocarbon cooling to 60 ℃, carry to the intermediate storage tank and store.
Preferably, the bottoms of the heavy oil separation tower 1, the heavy hydrocarbon separation tower 3 and the intermediate hydrocarbon separation tower 4 are respectively provided with a tower bottom reboiler 27, the bottom of the light hydrocarbon separation tower 2 is provided with a start-up reboiler 28, and the start-up reboiler 28 and the light hydrocarbon reboiler 26 are arranged in parallel; it should be noted that, the start-up reboiler 28 and the tower bottom reboiler 27 of this device all adopt conduction oil to heat, the separation of light hydrocarbon knockout tower 2 is in continuous operation after the start-up, switch to light hydrocarbon reboiler 26 by start-up reboiler 28, like this heavy oil knockout tower 1 of whole device, light hydrocarbon knockout tower 2, heavy hydrocarbon knockout tower 3 and middle hydrocarbon knockout tower 4 are in continuous operation, need not to set up other heat sources to the feeding again, be favorable to realizing reducing the energy consumption when the stable heavy oil of coal system separates into the alkene of narrow carbon number.
Preferably, the C5-8 mixed hydrocarbon gas phase outlet is sequentially connected with a C5-8 mixed hydrocarbon air cooler 29 and a C5-8 mixed hydrocarbon water cooler 30, the method comprises the steps that a C5-8 mixed hydrocarbon backflow tank 31 and a C5-8 mixed hydrocarbon backflow pump 32 are connected to a C9-11 mixed hydrocarbon conveying pump 33, a C9-11 mixed hydrocarbon air cooler 34 and a C9-11 mixed hydrocarbon water cooler 35 in sequence at a C9-11 mixed hydrocarbon liquid phase outlet, it is required to be noted that gas-phase C5-8 mixed hydrocarbon is cooled to 40 ℃ through the C5-8 mixed hydrocarbon air cooler 29 and the C5-8 mixed hydrocarbon water cooler 30, one part of the gas-phase C5-8 mixed hydrocarbon flows back under the conveying action of the C5-8 mixed hydrocarbon backflow pump 32, the other part of the gas-phase C9-11 mixed hydrocarbon is conveyed to a storage tank for storage, subsequent further upgrading processing is facilitated, and liquid-phase C9-11 mixed hydrocarbon is cooled to 40 ℃ through the C9-11 mixed hydrocarbon air cooler 34 and the C9-11 mixed hydrocarbon water cooler 35 and conveyed to the storage tank for storage, and subsequent further upgrading processing is facilitated.
Preferably, a heavy oil conveying pipe 36 is arranged at a feeding port of the heavy oil preheater 5, a heavy oil olefin coalescer 37 is arranged on the heavy oil conveying pipe 36, and the heavy oil olefin coalescer 37 mainly removes water in the coal-made stable heavy oil so as to avoid the influence of the water on vacuum rectification and the influence of the water on the quality of the product due to the reaction of the water and the coal-made heavy oil under the high-temperature action.
Preferably, the light hydrocarbon separation tower 2 is further provided with an oil-washed naphtha delivery pipe 38, and the oil-washed naphtha delivery pipe 38 is connected with the feed inlet of the light hydrocarbon separation tower 2 through the light hydrocarbon preheater 12.
Preferably, the oil-washed naphtha conveying pipe 38 is provided with an oil-washed naphtha olefin coalescer 39, and the oil-washed naphtha olefin coalescer 39 mainly removes water in the oil-washed naphtha so as to avoid the influence of the water on vacuum rectification and avoid the influence of the water and the oil-washed naphtha on the quality of the product due to the reaction under the action of high temperature.
It should be noted that, by mixing the oil-washed naphtha and the light hydrocarbon and then rectifying and separating the mixture in a light hydrocarbon separation tower, the device can effectively treat the oil-washed naphtha, which is beneficial to improving the added value of the oil-washed naphtha, and it should be further noted that the coal-made stable heavy oil is one of the intermediate products of the fischer-tropsch synthesis, and it can be understood that the coal-made stable heavy oil comes from a stripping tower in the fischer-tropsch synthesis process.
The olefin separation device takes coal-made stable heavy oil and oil-washed naphtha as raw materials, the yield of the obtained C5-8 mixed hydrocarbon is 17.93%, and the purity is more than or equal to 98%; the yield of the C9-11 mixed hydrocarbon is 11.03%, and the purity is more than or equal to 99%; the yield of the C12-13 mixed hydrocarbon is 6.65%, and the purity is more than or equal to 98%; the yield of the C14-17 mixed hydrocarbon is 29.48%, and the purity is more than or equal to 98%; the yield of the C19 heavier mixed hydrocarbon was 34.91%, and the C19 heavier mixed hydrocarbon had a C18 and lighter content of < 5%.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. An olefin separation device for upgrading coal-made stable heavy oil, which is characterized by comprising:
a heavy oil preheater (5) for preheating the coal-made heavy oil;
the heavy oil separation tower (1) is characterized in that the discharge port end of the heavy oil preheater (5) is connected with the middle part of the heavy oil separation tower (1), the heavy oil separation tower (1) is provided with a C11 and lighter hydrocarbon gas phase outlet and a C12 and heavier hydrocarbon outlet, and the top of the heavy oil separation tower (1) is provided with a first vacuum (6);
the device comprises a light hydrocarbon separation tower (2), wherein a C11 and lighter hydrocarbon gas-phase outlet is connected with the middle part of the light hydrocarbon separation tower (2) through a light hydrocarbon pipeline (7), a light hydrocarbon air cooler (8), a light hydrocarbon water cooler (9), a light hydrocarbon reflux tank (10), a light hydrocarbon reflux pump (11) and a light hydrocarbon preheater (12) are sequentially arranged on the light hydrocarbon pipeline (7), a C5-8 mixed hydrocarbon gas-phase outlet and a C9-11 mixed hydrocarbon liquid-phase outlet are arranged on the light hydrocarbon separation tower (2), and a first vacuum (6) is connected with the light hydrocarbon reflux tank (10);
heavy hydrocarbon knockout tower (3), heavy hydrocarbon knockout tower (3) are equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and heavier hydrocarbon liquid phase export, C12 and heavier hydrocarbon liquid phase export pass through heavy hydrocarbon pipeline (13) with the middle part of heavy hydrocarbon knockout tower (3) is connected, heavy hydrocarbon knockout tower (3) are equipped with C12 ~ 17 mixed hydrocarbon gaseous phase export and C19 and heavier hydrocarbon liquid phase export, heavy hydrocarbon knockout tower (3) top is equipped with second vacuum (14).
2. The olefin separation method for improving the quality of the coal-made stable heavy oil according to claim 1, further comprising an intermediate hydrocarbon separation tower (4) for separating C12-13 mixed hydrocarbons and C14-17 mixed hydrocarbons, wherein the C12-17 mixed hydrocarbon gas phase outlet is connected with the middle part of the intermediate hydrocarbon separation tower (4) through an intermediate hydrocarbon pipeline (15), the intermediate hydrocarbon separation tower (4) is provided with a C12-13 mixed hydrocarbon gas phase outlet and a C14-17 mixed hydrocarbon liquid phase outlet, the C12-13 mixed hydrocarbon gas phase outlet is sequentially connected with a C12-13 mixed hydrocarbon air cooler (16), a C12-13 mixed hydrocarbon reflux tank (17) and a C12-13 mixed hydrocarbon reflux pump (18), a third vacuum (19) is arranged at the top of the intermediate hydrocarbon separation tower (4), and the third vacuum (19) is connected with the intermediate hydrocarbon reflux tank (21).
3. The method for separating the olefins for improving the quality of the coal-made stable heavy oil according to claim 2, wherein an intermediate hydrocarbon air cooler (20), an intermediate hydrocarbon reflux tank (21), an intermediate hydrocarbon reflux pump (22) and an intermediate hydrocarbon preheater (23) are sequentially arranged on the intermediate hydrocarbon pipeline (15), the second vacuum (14) is connected with the intermediate hydrocarbon reflux tank (21), a C14-17 mixed hydrocarbon delivery pump (24) is connected to a C14-17 mixed hydrocarbon liquid phase outlet, and an outlet end of the C14-17 mixed hydrocarbon delivery pump (24) is connected with a heat source inlet of the intermediate hydrocarbon preheater (23) to serve as a heat source of the intermediate hydrocarbon preheater (23).
4. The olefin separation device for coal-to-liquids stable heavy oil upgrading according to claim 3, characterized in that the light hydrocarbon preheater (12) comprises a first preheater (121) and a second preheater (122), the first preheater (121) and the second preheater (122) are arranged in series on the light hydrocarbon pipeline (7), the heat source outlet of the intermediate hydrocarbon preheater (23) is connected with the heat source inlet of the first preheater (121), the liquid phase outlet of the C19 and heavier hydrocarbons is connected with a heavy hydrocarbon delivery pump (25), and the outlet end of the heavy hydrocarbon delivery pump (25) is connected with the heat source inlet end of the second preheater (122) to serve as the heat source of the second preheater (122).
5. The olefin separation device for upgrading the coal-made stable heavy oil as claimed in claim 4, wherein a light hydrocarbon reboiler (26) is arranged at the bottom of the light hydrocarbon separation tower (2), a heat source outlet of the light hydrocarbon reboiler (26) is connected with a heat source inlet of the second preheater (122), and an outlet end of the heavy hydrocarbon delivery pump (25) is connected with a heat source inlet of the light hydrocarbon reboiler (26).
6. The olefin separation device for improving the quality of the coal-made stable heavy oil according to claim 5, wherein the bottoms of the heavy oil separation tower (1), the heavy hydrocarbon separation tower (3) and the intermediate hydrocarbon separation tower (4) are provided with tower bottom reboilers (27), the bottom of the light hydrocarbon separation tower (2) is provided with a start-up reboiler (28), and the start-up reboiler (28) is connected with the light hydrocarbon reboiler (26) in parallel.
7. The olefin separation device for improving the quality of the coal-made stable heavy oil according to any one of claims 1 to 6, wherein the C5-8 mixed hydrocarbon gas phase outlet is sequentially connected with a C5-8 mixed hydrocarbon air cooler (29), a C5-8 mixed hydrocarbon water cooler (30), a C5-8 mixed hydrocarbon reflux tank (31) and a C5-8 mixed hydrocarbon reflux pump (32), and the C9-11 mixed hydrocarbon liquid phase outlet is sequentially connected with a C9-11 mixed hydrocarbon delivery pump (33), a C9-11 mixed hydrocarbon air cooler (34) and a C9-11 mixed hydrocarbon water cooler (35).
8. The olefin separation device for improving the quality of the coal-made stable heavy oil according to any one of claims 1 to 6, wherein a heavy oil conveying pipe (36) is arranged at a feeding port of the heavy oil preheater (5), and a heavy oil olefin coalescer (37) is arranged on the heavy oil conveying pipe (36).
9. The olefin separation device for improving the quality of the coal-made stable heavy oil according to any one of claims 1 to 6, wherein the light hydrocarbon separation tower (2) is further provided with an oil-washed naphtha delivery pipe (38), and the oil-washed naphtha delivery pipe (38) is connected with the feeding port of the light hydrocarbon separation tower (2) through the light hydrocarbon preheater (12).
10. The olefin separation device for upgrading of coal-derived stable heavy oil according to claim 9, characterized in that the oil-washed naphtha delivery pipe (38) is provided with an oil-washed naphtha olefin coalescer (39).
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