CN112457880A - Pre-lifting system and process of FCC (fluid catalytic cracking) device - Google Patents
Pre-lifting system and process of FCC (fluid catalytic cracking) device Download PDFInfo
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- 238000004231 fluid catalytic cracking Methods 0.000 title description 58
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Classifications
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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
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- 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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a pre-lifting system and a pre-lifting process of an FCC device, wherein low-carbon hydrocarbon is gasified under normal working conditions, and is superheated after being mixed with high-temperature steam and/or gas dry gas; before the mixture is input into the superheater, the mixing proportion of high-temperature steam and/or gas dry gas is gradually adjusted so as to avoid the occurrence of liquid or fog drops of the low-carbon hydrocarbon; after the gas is input into the superheater, the proportion and the flow of low-carbon hydrocarbon, high-temperature steam and/or gas dry gas are gradually adjusted again according to the working state of the pre-raiser, so that the lifting section of the FCC device works stably; the method comprises the following steps of firstly suspending low-carbon hydrocarbon input under the working condition of start-up, inputting high-temperature water vapor and/or dry gas into a pre-lifter, inputting low-carbon hydrocarbon into a gasifier for gasification after the pre-lifter reaches a preset working state, gradually increasing the flow of low-carbon hydrocarbon gas, and gradually adjusting the flow of the high-temperature water vapor and/or the dry gas before and after the low-carbon hydrocarbon gas is input into a superheater; obviously increases the economic benefit of the refinery and has the environmental protection effects of energy conservation and emission reduction.
Description
Technical Field
The invention relates to the field of conversion systems and processes in petroleum refineries, in particular to a pre-lifting system and a pre-lifting method for a fluid catalytic cracking unit.
Background
At present, in a pre-lifting section in a catalytic cracking process of a refinery, high-temperature steam and dry gas are mostly used as pre-lifting media, and the high-temperature steam, the dry gas or the combination of the high-temperature steam and the dry gas are generally adopted independently; because the high-temperature water vapor has the characteristics of safe and convenient production, the high-temperature water vapor is always used as a preferred medium for pre-lifting.
However, after the high-temperature steam enters the pre-lifting section, the hydrothermal deactivation speed of the catalyst is increased to a certain extent, the thermal collapse and aging of the catalyst are accelerated, the consumption of the catalyst and the high-temperature steam is increased, and the condenser load and the acid water discharge amount at the top of the fractionating tower are increased.
The gas dry gas takes hydrogen, methane and a small amount of ethane as main bodies, and if the gas dry gas is taken as a pre-lifting medium, the components of the gas dry gas are unstable, the pressure is greatly influenced by the outlet environment of a compressor and a system pipe network, and the gas dry gas is an inert component of catalytic cracking reaction and occupies the reaction activity center of a catalytic cracking agent.
In view of the fact that the temperature of the pre-lifting medium for catalytic cracking is lower than 300 ℃, an assumption that liquid hydrocarbons, light oil and heavy oil are atomized by high-temperature steam to be used as the pre-lifting medium has been proposed, but various problems possibly caused by the atomization are not listed, analyzed and solved, and no practical application case exists so far.
Therefore, there is still a need for improvement and development of the prior art.
Disclosure of Invention
In order to solve the technical problems, the invention provides a pre-lifting system of an FCC device, which can obviously increase the economic benefit of a refinery and has the environment-friendly effects of energy conservation and emission reduction.
Meanwhile, the invention also provides a pre-upgrading process of the FCC device, which can obviously increase the economic benefit of refineries and is beneficial to having the environment-friendly effects of energy conservation and emission reduction.
The technical scheme of the invention is as follows: a pre-lift process for an FCC unit, wherein:
under normal working conditions, firstly, inputting low-carbon hydrocarbon into a gasifier for gasification, then, controlling pressure, mixing the low-carbon hydrocarbon with high-temperature steam and/or gas dry gas, inputting the mixture into a superheater for overheating, and finally, inputting the mixture into a pre-raiser;
before the low-carbon hydrocarbon is input into the superheater, the mixing proportion and the respective flow rate of high-temperature steam and/or gas dry gas are gradually adjusted according to the coking difficulty of the low-carbon hydrocarbon at high temperature, so that the phenomenon of liquid state or fog drop of the low-carbon hydrocarbon is avoided;
after the gas is input into the superheater, the proportion and the flow of the low-carbon hydrocarbon, the high-temperature steam and/or the gas dry gas are gradually adjusted again according to the working state of the pre-raiser, so that the lifting section of the FCC device works stably;
under the working condition of start-up, the low-carbon hydrocarbon is input into the gasifier for gasification, only high-temperature water vapor and/or dry gas are input into the pre-lifter, after the pre-lifter reaches a preset working state, the low-carbon hydrocarbon is input into the gasifier for gasification, the flow of the low-carbon hydrocarbon gas is gradually increased, and the flow of the high-temperature water vapor and/or the dry gas before and after the low-carbon hydrocarbon gas is input into the superheater is gradually adjusted.
The pre-lifting process of the FCC unit, wherein: when the gasifier fails under normal working conditions and needs to be overhauled on line, high-temperature steam and/or dry gas are only input into the pre-lifting device after passing through the heat device, so that the gasifier can be conveniently switched out from the system on line for overhauling, and the gasifier is switched in on line after overhauling.
The pre-lifting process of the FCC unit, wherein: when the superheater fails under normal working conditions and needs to be overhauled on line, only high-temperature steam and/or dry gas are input into the pre-raiser, so that the superheater can be cut out from the system on line for overhauling, and the superheater is cut in line after overhauling.
The pre-lifting process of the FCC unit, wherein: the gasifier adopts a pressure control mode, the superheater adopts a temperature control mode, and the flow control mode of related input pipelines is combined to realize the accurate control of the pressure, the temperature and the flow of the low-carbon hydrocarbon components.
The pre-lifting process of the FCC unit, wherein: and a heat source for heating the gasifier and/or the superheater directly or indirectly comes from a heating furnace, high-temperature water vapor, heat transfer oil, a thermal catalyst or a burning energy of a catalyst regenerator or superheated high-temperature water vapor of an internal heat remover and an external heat remover of the catalyst regenerator.
The pre-lifting process of the FCC unit, wherein: the low-carbon hydrocarbon comprises one or more of ethane, propane, isobutane, ethylene-rich gas, normal isobutane, normal isobutene, carbon three, carbon four, carbon five, carbon six, carbon seven, carbon eight and carbon nine; and the lower hydrocarbon comprises one or more components of saturated hydrocarbon, naphthenic hydrocarbon, olefin or aromatic hydrocarbon.
A pre-lift system for an FCC unit comprising input lines and valves thereof disposed between a gasifier, a superheater and a pre-lift, wherein:
a first input line for inputting low-carbon hydrocarbon to the gasifier is arranged at one side of the gasifier;
a second input pipeline for inputting a gasification state pre-lifting medium to the superheater is arranged between the gasifier and the superheater, and a second front valve is arranged on the second input pipeline;
a third input pipeline for inputting the gasified and superheated pre-lifting medium to the pre-lifter is arranged between the superheater and the pre-lifter, and a third valve is arranged on the third input pipeline;
the second input pipeline is provided with an input pipeline for inputting high-temperature water vapor and/or gas dry gas and a valve thereof;
an input pipeline for inputting high-temperature water vapor and/or gas dry gas and a valve thereof are arranged on the third input pipeline;
along the flowing direction of the gasification state pre-lifting medium, the second front valve, the joint of the input pipeline of the high-temperature water vapor and the second input pipeline, and the joint of the input pipeline of the gas dry gas and the second input pipeline are sequentially positioned on the second input pipeline;
along the flowing direction of the gasified and overheated pre-lifting medium, the third valve, the joint of the input pipeline of the high-temperature water vapor and the third input pipeline, and the joint of the input pipeline of the gas dry gas and the third input pipeline are sequentially positioned on the third input pipeline.
The pre-lift system of an FCC unit, wherein: and the first input pipeline is provided with a first valve which is used for being matched with a second front valve on a second input pipeline to be independently switched on or switched off the gasifier on line.
The pre-lift system of an FCC unit, wherein: ninth input pipelines are connected in parallel to two sides of the superheater to replace a seventh input pipeline arranged on the third input pipeline, and a second rear valve is arranged on the second input pipeline and is used for being matched with a third valve to independently cut out or cut out the superheater on line; and a ninth valve is arranged on the ninth input pipeline to replace the seventh valve arranged on the seventh input pipeline;
along the flowing direction of the gasification state pre-lifting medium, a second front valve, the joint of the input pipeline of the high-temperature water vapor and the second input pipeline, the joint of the input pipeline of the gas dry gas and the second input pipeline, the joint of the ninth input pipeline and the second input pipeline, and a second rear valve are sequentially positioned on the second input pipeline;
along the flowing direction of the gasified and overheated pre-lifting medium, the third valve, the joint of the ninth input pipeline and the third input pipeline, the joint of the input pipeline of the high-temperature water vapor and the third input pipeline, and the joint of the input pipeline of the gas dry gas and the third input pipeline are sequentially positioned on the third input pipeline.
The pre-lift system of an FCC unit, wherein: an eighth input pipeline for inputting high-temperature water vapor is arranged on the third input pipeline to replace a fifth input pipeline arranged on the third input pipeline, and an eighth valve is arranged on the eighth input pipeline to replace a fifth valve arranged on the fifth input pipeline; along the flowing direction of the gasified and overheated state pre-lifting medium, the third valve, the connection part of the seventh input pipeline and the third input pipeline and the connection part of the eighth input pipeline and the third input pipeline are sequentially positioned on the third input pipeline.
Compared with the prior art, the pre-lifting system and the pre-lifting process of the FCC device provided by the invention have the following advantages:
1. the integral high-temperature steam consumption of the FCC device and the hydrothermal deactivation rate of the catalyst are obviously reduced, the consumption of fresh catalyst is obviously reduced, the material loss and energy consumption of the FCC device in the catalytic cracking reaction process are also reduced, the emission and treatment of acid water are obviously reduced, and the energy conservation and emission reduction are effectively achieved;
2. the effective treatment capacity of the catalytic cracking device is obviously improved, the low-carbon hydrocarbon is used as a pre-lifting medium, high-value components such as low-carbon olefin, hydrogen and the like are greatly increased, and the benefit of the catalytic cracking device is obviously improved;
3. the temperature reduction of the regenerated catalyst caused by the contact of the pre-lifting medium and the regenerated catalyst is obviously reduced, the temperature of the regenerated catalyst is improved, the depth of catalytic cracking or catalytic cracking reaction is facilitated, and the low-carbon olefin is greatly increased.
Drawings
The drawings described herein are for illustration purposes only and are not intended to limit the scope of the present disclosure in any way; the shapes, the proportional sizes, and the like of the respective members in the drawings are merely schematic for aiding the understanding of the present invention, and do not specifically limit the shapes, the proportional sizes, and the like of the respective members of the present invention; those skilled in the art, having the benefit of the teachings of this invention, may choose from the various possible shapes and proportional sizes to implement the invention as a matter of case.
FIG. 1 is a schematic diagram of a pre-lift system and process embodiment of an FCC unit of the present invention;
FIG. 2 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the sixth input line and its sixth valve omitted);
FIG. 3 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the fourth input line and its fourth valve omitted);
FIG. 4 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the seventh input line and its seventh valve deleted);
FIG. 5 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the fifth input line and its fifth valve omitted);
FIG. 6 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the eighth input line and its eighth valve omitted);
FIG. 7 is a schematic diagram of a pre-lift system and process embodiment of the FCC unit of the present invention (with the fifth input line and its fifth valve omitted);
FIG. 8 is a schematic diagram of a pre-lift system and process embodiment of an FCC unit of the invention (omitting the sixth input line and its sixth valve, the seventh input line and its seventh valve, the eighth input line and its eighth valve);
the various reference numbers in the figures are summarized: gasifier 100, superheater 200, pre-riser 300, first input line 410, first valve 411, second input line 420, second front valve 421, second rear valve 422, third input line 430, third valve 431, fourth input line 440, fourth valve 441, fifth input line 450, fifth valve 451, sixth input line 460, sixth valve 461, seventh input line 470, seventh valve 471, eighth input line 480, eighth valve 481, ninth input line 490, ninth valve 491.
Detailed Description
The embodiments and examples of the present invention will be described in detail below with reference to the accompanying drawings, and the described embodiments are only for the purpose of illustrating the present invention and are not intended to limit the embodiments of the present invention.
The invention relates to a pre-lifting system and a process of an FCC device, belonging to the field of petrochemical industry, wherein an FCC (Fluid catalytic cracking, also called Fluid-bed catalytic cracking, or Fluid catalytic cracking, Chinese name: Fluid catalytic cracking, for short: catalytic cracking) process is one of the most important conversion processes in petroleum refineries and is widely used for converting hydrocarbon components with high boiling point and high molecular weight in petroleum crude oil into more valuable gasoline, olefin gas and other products; cracking of petroleum hydrocarbons is initially accomplished by thermal cracking; thermal cracking has now been almost entirely replaced by catalytic cracking, which can produce more gasoline with a high octane number; in addition, because catalytic cracking also produces more byproduct gases having carbon-carbon double bonds (i.e., more olefins), catalytic cracking processes have a higher economic value than thermal cracking processes; the FCC unit to which the process refers includes fluid catalytic cracking and catalytic cracking units as is normally understood.
Referring to fig. 1, fig. 1 is a schematic diagram of a pre-lift system and process embodiment of an FCC unit of the present invention, including input lines and valves thereof disposed between a gasifier 100, a superheater 200 and a pre-lift 300:
a first input line 410 for inputting low carbon hydrocarbons to the gasifier 100 is provided at one side of the gasifier 100;
a second input line 420 is provided between the gasifier 100 and the superheater 200 for inputting the pre-lifting medium in a gasified state to the superheater 200; the second input pipeline 420 is provided with a second front valve 421 for gradually adjusting the flow of the gasified low-carbon hydrocarbon output by the gasifier 100 and for matching with other valves to cut or cut into the gasifier 100 when the gasifier 100 is independently overhauled on line;
a third input line 430 is provided between the superheater 200 and the pre-lifter 300 for inputting the vaporized, superheated pre-lifting medium to the pre-lifter 300; and the third input line 430 is provided with a third valve 431 for switching in or out the superheater 200 in cooperation with other valves when the superheater 200 is overhauled on line;
a fourth input line 440 and a fifth input line 450 are respectively arranged on the second input line 420 and the third input line 430, and are respectively used for inputting high-temperature water vapor into the second input line 420 and the third input line 430 and heating the low-carbon hydrocarbon gas so as to utilize the high-temperature water vapor to inhibit or prevent the coking phenomenon of the low-carbon hydrocarbon when the low-carbon hydrocarbon is overheated in the superheater 200; a fourth valve 441 is disposed on the fourth input pipeline 440, and is used for gradually adjusting the flow of the high-temperature steam input into the second pipeline 420; and a fifth valve 451 is provided on the fifth input line 450 for gradually adjusting the flow rate of the high-temperature steam inputted into the third line 430;
a sixth input pipeline 460 and a seventh input pipeline 470 are respectively arranged on the second input pipeline 420 and the third input pipeline 430, and are respectively used for inputting the gas dry gas into the second input pipeline 420 and the third input pipeline 430 so as to utilize inert components such as methane in the gas dry gas to inhibit or prevent the low-carbon hydrocarbon from coking when the superheater 200 is overheated; and the sixth input line 460 is provided with a sixth valve 461 for adjusting the flow rate of the gas dry gas gradually input into the second line 420; and the seventh input line 470 is provided with a seventh valve 471 for stepwise adjusting the flow rate of the gas dry gas input to the third line 430.
It should be noted that, since the low-carbon hydrocarbons can be prevented from being liquid or fogged to different degrees by only inputting high-temperature steam or only inputting gas dry gas before being inputted into the superheater 200, as an alternative to the deletion of the part of fig. 1 before the superheater 200, without considering other variables, in conjunction with fig. 2 and 3, fig. 2 is a schematic diagram of the pre-lift system and process embodiment (deleting the sixth input line and its sixth valve) of the FCC unit of the present invention, fig. 3 is a schematic diagram of the pre-lift system and process embodiment (deleting the fourth input line and its fourth valve) of the FCC unit of the present invention, and the fourth input line 440 and its fourth valve 441 and the sixth input line 460 and its sixth valve 461 can be selected alternatively, and in the case of having both the fourth valve 441 and the sixth input line 460 and its sixth valve 461, the adjusting process is more variable and fine, and the adjusting effect is better; in addition, the deletion replacement scheme of the part can be combined with the deletion replacement scheme of other parts to form a new embodiment, and further description is omitted here.
Similarly, as the deletion alternative of fig. 1 after the superheater 200 can stabilize the operation of the lift section of the FCC unit to different degrees by only inputting high-temperature steam or only inputting gas dry gas, in conjunction with fig. 4 and 5, fig. 4 is a schematic diagram of the pre-lift system and process embodiment (deleting the seventh input line and its seventh valve) of the FCC unit of the present invention, and fig. 5 is a schematic diagram of the pre-lift system and process embodiment (deleting the fifth input line and its fifth valve) of the FCC unit of the present invention, the fifth input line 450 and its fifth valve 451 and the seventh input line 470 and its seventh valve 471 can be selected alternatively, and in the case of having both the fifth input line 450 and its fifth valve 451 and the seventh input line 470 and its seventh valve 471, the adjusting process is more variable and fine, and the adjusting effect is better; in addition, the deletion replacement scheme of the part can be combined with the deletion replacement scheme of other parts to form a new embodiment, and further description is omitted here.
An eighth input line 480 for separately inputting high-temperature steam is further provided on the third input line 430; an eighth valve 481 is arranged on the eighth input pipeline 480 and is used for quantitatively adjusting the flow of the high-temperature steam input into the pre-lifter 300;
it should be noted that, since the eighth input line 480 has the same regulating function as the fifth input line 450, and can input the high-temperature steam into the third input line 430 after the superheater 200, as an alternative to the deletion of the high-temperature steam input portion in fig. 1, without considering other variables, in combination with fig. 6 and 7, fig. 6 is a schematic diagram of the pre-lift system and process embodiment of the FCC unit of the present invention (deleting the eighth input line and its eighth valve), fig. 7 is a schematic diagram of the pre-lift system and process embodiment of the FCC unit of the present invention (deleting the fifth input line and its fifth valve), the eighth input line 480 and its eighth valve 481 can be replaced or selected from the fifth input line 450 and its fifth valve 451, and in the case of both the fifth input line 450 and its fifth valve 451 and the eighth input line 480 and its eighth valve 481, the adjustment process is more variable and fine, and the influence on the pre-lifter 300 is also smaller; in addition, the deletion replacement scheme of the part can be combined with the deletion replacement scheme of other parts to form a new embodiment, and further description is omitted here.
For example, with reference to fig. 8, fig. 8 is a schematic diagram of a pre-lift system and process embodiment of an FCC unit of the present invention (with the sixth input line and its sixth valve, the seventh input line and its seventh valve, and the eighth input line and its eighth valve omitted); the technical scheme is a new embodiment formed by combining the deletion alternative of the part of the superheater 200 in the figure 1 and the deletion alternative of the part of the superheater 200 in the figure 1 with the deletion alternative of the part of the superheater 200 to which the high-temperature steam is input.
In the flow direction of the gasification state pre-lifting medium, i.e. from the gasifier 100 to the superheater 200: the second front valve 421, the connection of the fourth input pipeline 440 and the second input pipeline 420, and the connection of the sixth input pipeline 460 and the second input pipeline 420 are sequentially located on the second input pipeline 420;
in the flow direction of the gasified and superheated pre-lift medium, i.e. from the superheater 200 to the pre-lift 300: the third valve 431, the connection of the fifth input line 450 to the third input line 430, the connection of the seventh input line 470 to the third input line 430, and the connection of the eighth input line 480 to the third input line 430 are located in sequence on the third input line 430.
The pre-lifting system of the FCC device can effectively solve the problems that the pre-lifting system of the FCC device is unstable in operation, heating parts are easy to coke and are not easy to operate for a long time when low-carbon hydrocarbons are used as pre-lifting media, and the normal operation of the FCC device is influenced by the overhaul of a heater once the heater is coked.
To facilitate the separate online maintenance of the gasifier 100, it is preferable that the first input line 410 is provided with a first valve 411 for matching with a second front valve 421 on the second input line 420 to cut out the gasifier 100 on line for maintenance and then cut into the gasifier 100 on line after maintenance, so as to ensure that the superheater 200 and the pre-lifter 300 are both in normal working condition during the maintenance of the detached gasifier 100; meanwhile, the first valve 411 is also used to gradually adjust the flow of the gasified low-carbon hydrocarbon fed into the gasifier 100 under normal conditions.
To facilitate the individual online maintenance of the superheater 200, it is preferable that a ninth input line 490 is connected in parallel to both sides of the superheater 200, and a second back valve 422 is provided on the second input line 420 for cooperating with the third valve 431 to cut the superheater 200 on-line for maintenance and then cut into the superheater 200 on-line after maintenance; and a ninth valve 491 is provided on the ninth input line 490 for maintaining stable operation of the gasifier 100 and the pre-lifter 300 under abnormal conditions during maintenance of the removed superheater 200.
Thus, the positional relationship of the associated line connections and valves on the second input line 420, in the flow direction of the gasification pre-lift medium, i.e. from the gasifier 100 to the superheater 200, is as follows: a second front valve 421, a junction of the fourth input line 440 and the second input line 420, a junction of the sixth input line 460 and the second input line 420, a junction of the ninth input line 490 and the second input line 420, a second rear valve 422;
and the position relationship of the relevant line connections and valves on the third input line 430 in the flow direction of the gasified and superheated pre-lift medium, i.e., the direction from the gasifier 100 to the superheater 200, are as follows: a third valve 431, a connection of a ninth input line 490 to the third input line 430, a connection of a fifth input line 450 to the third input line 430, a connection of a seventh input line 470 to the third input line 430, and a connection of an eighth input line 480 to the third input line 430.
It should be noted that, in the case of the ninth input line 490 connected in parallel to the both sides of the superheater 200, as an alternative to the deletion of the dry gas part of the input gas in fig. 1, the ninth input line 490 and its ninth valve 491 can replace the seventh input line 470 and its seventh valve 471 without considering other variation factors, as shown in fig. 4, after the input of the superheater 200, the lifting section of the FCC unit can be operated stably by only inputting the dry gas, and in the case of both the seventh input line 470 and its seventh valve 471 and the ninth input line 490 and its ninth valve 491, the adjustment process can be more variable and finer and the effect on the pre-lift 300 can be smaller; in addition, the deletion replacement scheme of the part can be combined with the deletion replacement scheme of other parts to form a new embodiment, and further description is omitted here.
To facilitate gasification of the lower hydrocarbons, the other end of the first input line 410 is preferably in communication with a pressure booster (not shown) for further pressurizing or pressurizing the lower hydrocarbons for input to the gasifier 100.
Preferably, a raw material return line (not shown) is further provided in the gasifier 100 for discharging high boiling point materials enriched in the gasifier 100 after a certain period of operation, so as to reduce a small amount of relatively high boiling point materials possibly mixed in the low carbon hydrocarbons.
Based on the pre-lifting system of the FCC device, the invention also provides a pre-lifting process or method of the FCC device, which comprises the following steps:
under normal working conditions, firstly inputting low-carbon hydrocarbon (or the low-carbon hydrocarbon after pressure increase) into a gasifier 100 for gasification, then inputting the mixture into a superheater 200 for overheating after being mixed with high-temperature steam and/or gas through pressure control, and finally inputting the mixture into a pre-lifter 300; during normal operation, the ninth valve 491 on the ninth input line 490 is always closed;
before the low-carbon hydrocarbon is input into the superheater 200, the mixing proportion and the respective flow rate of the high-temperature steam and/or the dry gas are gradually adjusted by gradually adjusting a fourth valve 441 on a fourth input pipeline 440 and a sixth valve 461 on a sixth input pipeline 460 according to the difficulty of coking of the low-carbon hydrocarbon at high temperature, and the adjustment is carried out according to the principle that the overall temperature of the mixed gas needs to exceed the boiling temperature of the low-carbon hydrocarbon under the pressure in a second pipeline 420, so as to avoid the liquid or fog drop phenomenon of the low-carbon hydrocarbon; inert components such as methane and the like in the high-temperature steam and the gas dry gas are used as coking inhibition components, and two or only one of the inert components can be input at the same time;
after being input into the superheater 200, the proportion and flow rate of the low-carbon hydrocarbon, the high-temperature steam and/or the gas dry gas are gradually adjusted again by gradually adjusting the fifth valve 451 on the fifth input line 450 and the seventh valve 471 on the seventh input line 470 according to the working state of the pre-riser, so as to stabilize the operation of the lift section of the FCC unit; under different working conditions, except low-carbon hydrocarbon, the content proportion adjustment range of the high-temperature water vapor and the gas dry gas in the mixed gas is between 0 and 100 percent;
under the working condition of start-up, firstly suspending the low-carbon hydrocarbon input into the gasifier 100 for gasification, only inputting high-temperature steam and/or dry gas into the pre-lifter 300 after the high-temperature steam and/or dry gas is overheated by the heater 200, namely closing the first valve 411 on the first input pipeline 410 and the second front valve 421 on the second input pipeline 420, opening the second rear valve 422 on the second input pipeline 420 and the third valve 431 on the third input pipeline 430, and preheating the superheater 200 and the pre-lifter 300 by opening and adjusting the fourth valve 441 on the fourth input pipeline 440; after the pre-lifter 300 reaches a preset or expected working state, the gasifier 100 is started, i.e., the first valve 411 on the first input pipeline 410 is opened, the low carbon hydrocarbon (or the pressurized low carbon hydrocarbon) is input into the gasifier 100 for gasification, the flow of the low carbon hydrocarbon gas is gradually increased by gradually adjusting the second front valve 421 on the second input pipeline 420 and the first valve 411 on the first input pipeline 410, and the flow of the high temperature steam and/or the gas dry gas input into the second pipeline 420 is gradually adjusted by gradually adjusting the fourth valve 441 on the fourth input pipeline 440 and/or the sixth valve 461 on the sixth input pipeline 460; and gradually adjusting the flow of the high-temperature steam and/or the gas dry gas input into the third pipeline 430 by gradually adjusting the fifth valve 451 on the fifth input pipeline 450 and/or the seventh valve 471 on the seventh input pipeline 470, so as to achieve the purposes of increasing the yield of the low-carbon olefins, reducing the coking of the superheater and reducing the hydrothermal disintegration of the catalyst, and achieve comprehensive optimization; the ninth valve 491 on the ninth input line 490 is also always closed during start-up conditions.
According to the pre-lifting process or method of the FCC device, low-carbon hydrocarbon enters a gasifier 100 after being subjected to pressure lifting, the gasified low-carbon hydrocarbon flows into a superheater 200 through pressure control (namely pressure control), and high-temperature steam and gas dry gas in a proper proportion are mixed according to the difficulty of coking of the low-carbon hydrocarbon at high temperature before flowing into the superheater 200 so as to ensure that the low-carbon hydrocarbon does not have the phenomena of liquid state, fog drops and the like before entering the superheater 200; after passing through the superheater 200, the proportion of subsequently added high-temperature steam and gas dry gas is determined according to the working state of the pre-lift 300; therefore, the heating process of the low-carbon hydrocarbon is divided into two links of gasification and overheating, after the gasification process, according to the characteristics of the used low-carbon hydrocarbon, the proper high-temperature steam and/or gas dry gas are considered to be mixed, and the heating process is taken as an effective means for inhibiting the low-carbon hydrocarbon from coking in the superheater 200, so that the problems that the operation of the pre-lifting system of the FCC device is unstable, a heating part is easy to coke and is not easy to operate for a long time, which are faced by using the low-carbon hydrocarbon as a pre-lifting medium, and the normal operation of the FCC device is influenced by the overhaul of the heater once after coking are.
Further, when the gasifier 100 and/or the superheater 200 are out of order under normal operating conditions and need to be overhauled online (i.e., overhauled without shutdown of the pre-riser 300), only high-temperature steam and/or gas dry gas (after being superheated by the heater 200) is input into the pre-riser 300 so as to avoid affecting the long-term operation of the FCC unit, and the gasifier 100 and/or the superheater 200 can be switched out of the system online for overhauling, and the gasifier 100 and/or the superheater 200 can be switched in line after overhauling;
specifically, if the gasifier 100 is to be cut in or cut out separately during normal operating conditions, only the first valve 411 on the first input line 410 and the second front valve 421 on the second input line 420 need to be closed, so as to stably maintain the long-period operation of the superheater 200 and the pre-lifter 300, and significantly reduce the shutdown loss of the refinery;
specifically, if the superheater 200 is to be cut-in or cut-in separately during normal operating conditions, the second post-valve 422 on the second input line 420 and the third valve 431 on the third input line 430 need to be closed, and the ninth valve 491 on the ninth input line 490 needs to be opened and gradually adjusted, so as to stably maintain the long-term operation of the gasifier 100 and the pre-booster 300, and the production down-stream loss of the refinery can be significantly reduced.
Preferably, the gasifier 100 employs a pressure (and temperature) control method, and the superheater 200 employs a temperature control method, in combination with a flow control method of a relevant input pipeline, to achieve accurate control of the pressure, temperature, and flow of the low-carbon hydrocarbon component by the whole FCC unit; meanwhile, the eighth input pipeline 480 which is independently reserved with high-temperature water vapor as a pre-lifting medium can adopt one pipeline for flow fixation and the other pipeline for flow adjustment in actual operation, so that more accurate control of the lifting medium can be realized, and the problem that the flow of the lifting medium is great is avoided as much as possible.
Specifically, under normal working conditions, the operating pressure of the gasifier 100 is controlled to be between 0.3 Mpa and 2.0Mpa during the gasification process of the low-carbon hydrocarbons, so that the low-carbon hydrocarbons reach the boiling temperature thereof under the operating pressure; and the low-carbon hydrocarbon, the high-temperature steam and the gas dry gas before entering the superheater 200 are all in a gaseous state through temperature control, so that the phenomenon of liquid drop or atomization cannot occur.
Specifically, under normal working conditions, in the process of superheating the low-carbon hydrocarbons, the operating temperature of the superheater 200 is greater than 100 ℃ and less than 650 ℃, so that the mixed gas of the low-carbon hydrocarbons, the high-temperature steam and the gas dry gas is in a superheated state after passing through the superheater 200.
Under the working condition of start-up, firstly, high-temperature water vapor and gas dry gas are utilized to realize the stability of the pre-lifting medium, wherein the superheater 200 can be preheated by utilizing the high-temperature water vapor firstly, and after the system is stabilized, the low-carbon hydrocarbon is gradually gasified and superheated by adjusting the heat sources of the gasifier 100 and the superheater 200, so that the low-carbon hydrocarbon gas is merged into the pre-lifting medium by adopting a method with least disturbance.
In the entire pre-lift system, the heat source for gasifying and superheating the liquid hydrocarbon (i.e., heating the gasifier 100 and/or the superheater 200) may come directly or indirectly from a heating furnace, high-temperature steam, heat transfer oil, or directly or indirectly from the hot catalyst or coke-burning energy of the catalyst regenerator, including but not limited to superheated high-temperature steam from the internal and external heat collectors of the catalyst regenerator; and the heat source can adopt a single form or a combination form of a plurality of heat sources.
It should be noted that the lower part of the pre-riser 300 adopted in the FCC unit of the present invention is a pre-riser section, and the lower part of the pre-riser section can be provided with distribution pipes, which can be respectively communicated with the feed pipe of the dry gas, the feed pipe of the superheated high-temperature steam and the feed pipe of the gasified low-carbon hydrocarbon; the three feeding pipes can be simplified into a combination that any two materials are combined and then communicated with the third material, or the three materials are directly communicated and combined and then communicated with the distribution pipe; when the device is simplified, a mixer for three materials or any two materials of high-temperature steam, dry gas of gas and gasified low-carbon hydrocarbon can be arranged before entering the distribution pipe, or an input pipeline for communicating the three materials or any two materials of high-temperature steam, dry gas of gas and gasified low-carbon hydrocarbon is directly arranged without a special mixer, and the input pipeline is separated by a valve; alternatively, the feed lines for the three materials to be kept separately can also be connected directly to the distributor pipe without simplification.
The pre-lifting gas entering the pre-lifting section can be single gaseous low-carbon hydrocarbon or mixed gas mixed with high-temperature water vapor and gas dry gas, and the mass ratio of the high-temperature water vapor, the gas dry gas and the low-carbon hydrocarbon can be 0-100% in order to reduce coking of the heat exchange tube wall of the low-carbon hydrocarbon caused by the high temperature of the low-carbon hydrocarbon through the superheater 200.
The low-carbon hydrocarbon used in the invention comprises one or more combinations of light hydrocarbons such as ethane, propane, isobutane, ethylene-rich gas, normal isobutane, normal isobutene, carbon three, carbon four, carbon five, carbon six, carbon seven, carbon eight, carbon nine and the like, and mixed liquefied gas mainly containing carbon three and carbon four, wherein the combination proportion can be any proportion between 0 and 100 percent; and the lower hydrocarbon comprises one or more components of saturated hydrocarbon, naphthenic hydrocarbon, olefin or aromatic hydrocarbon.
It is recommended that the pre-lift media, such as low carbon hydrocarbons, high temperature steam, dry gas, etc., be heated to a temperature that is compatible with (i.e., as close as possible to) the temperature of the regenerated catalyst used, and that the gaseous low carbon hydrocarbons be at a temperature in excess of 100 ℃ when entering the bottom of the pre-lift 300; different final superheating temperatures can be adopted for different low-carbon hydrocarbons; the superheated mixed gas is then used as all or part of the pre-lift medium.
Taking a certain catalytic cracking device as an example, the temperature of the regenerated catalyst returned by a bottom regenerator (not shown in the figure) is 680 ℃, and the circulation amount is 1350 tons/hour; the original pre-lifting medium is normal temperature, 1.0MPa, 2000nm3Gas dry gas per hour and superheated high-temperature steam with the temperature of 290 ℃, the pressure of 1.0MPa and the pressure of 5 t/hour.
Example 1, by using the pre-lifting system and process of the present invention, 3 tons of propane are used as a low carbon hydrocarbon main body, after the propane passes through the gasifier 100, high temperature water vapor is mixed according to a mass ratio of 1:1, after the propane passes through the superheater 200, the mixture is adjusted to 1.0MPa, 450 ℃, 6t/h of gasified propane + high temperature water vapor, and then the mixture is mixed with 1.0MPa, 290 ℃, 1.2t/h of superheated high temperature water vapor to be input into the pre-lifter 300 as a pre-lifting medium;
under normal conditions, about 60% of propane is converted, with about 15% of methane, about 20% of ethylene, about 22% of propylene and about 2% of hydrogen;
for this catalysis, 0.6 ton more ethylene and 0.66 ton more propylene per hour were produced, otherwise unchanged; according to the calculation that the value of the low-carbon olefin is 3000 yuan/ton higher than that of the liquefied gas, the income is increased by about 3780 yuan per hour, namely about 9.07 ten thousand yuan per day, or about 63.5 ten thousand yuan per week, and the economic efficiency is remarkable; in addition, the yield of the acid water converted by the high-temperature steam is reduced by 0.8t/h, namely 19.2 tons/day or 134.4 tons/week, and the environmental protection benefit is obvious.
Embodiment 2, adopting the pre-lifting system and process of the present invention, 3 tons of isobutane is used as the main body of the low carbon hydrocarbon, after the isobutane passes through the gasifier 100, high temperature water vapor is mixed according to the mass ratio of 1:1, after passing through the superheater 200, the mixture is adjusted to 1.0MPa, 450 ℃, 6t/h gasified isobutane + high temperature water vapor, and then 1.0MPa, 290 ℃, 1.4t/h superheated high temperature water vapor is mixed as the pre-lifting medium and is input into the pre-lifter 300;
under normal conditions, about 70% of isobutane is converted, wherein the yield of methane is about 22%, the yield of ethylene is about 12%, the yield of ethane is about 6%, the yield of propylene is about 24%, the yield of propane is about 7%, and the yield of hydrogen is about 2%;
for this catalysis, 0.36 ton more ethylene and 0.72 ton more propylene per hour were produced, otherwise unchanged; according to the calculation that the value of the low-carbon olefin is 3000 yuan/ton higher than that of the liquefied gas, the income is increased by about 3240 yuan per hour, namely about 7.78 ten thousand yuan per day, or about 54.4 ten thousand yuan per week, and the economic efficiency is remarkable; in addition, the yield of the acid water converted by the high-temperature steam is reduced by 1.0t/h, namely 24 tons/day or 168 tons/week, and the environmental protection benefit is obvious.
It should be understood that the above-mentioned embodiments are merely preferred embodiments of the present invention, and are not intended to limit the technical solutions of the present invention, and those skilled in the art can add, subtract, replace, change or modify the above-mentioned embodiments within the spirit and principle of the present invention; for example, in the case of deleting the eighth input line 480 and the eighth valve 481, the seventh valve 471 may be provided on the seventh input line 470 only in combination, or the sixth input line 460 and the sixth valve 461 only in combination, or the fourth input line 440 and the fourth valve 441 only in combination; for another example, in order to separately overhaul the superheater 200 on line, the ninth input line 490 and the ninth valve 491 thereof are not connected in parallel to both sides of the superheater 200, but a backup superheater is connected in parallel to replace the superheater 200 to be overhauled on line; as another example, in embodiments where there is no dry gas input at all, both the sixth input line 460 and its sixth valve 461, and the seventh input line 470 and its seventh valve 471, are eliminated; in addition, the gasifier 100 and the superheater 200 in the figure can be two independent devices, or can be one device combining two sections of gasification and superheating, such as a gasification superheater disclosed in application publication No. CN 101995173A; and the like, and all such additions, substitutions, modifications and improvements may be made without departing from the scope of the invention as defined in the accompanying claims.
Claims (10)
1. A pre-lifting process of an FCC unit, comprising:
under normal working conditions, firstly, inputting low-carbon hydrocarbon into a gasifier for gasification, then, controlling pressure, mixing the low-carbon hydrocarbon with high-temperature steam and/or gas dry gas, inputting the mixture into a superheater for overheating, and finally, inputting the mixture into a pre-raiser;
before the low-carbon hydrocarbon is input into the superheater, the mixing proportion and the respective flow rate of high-temperature steam and/or gas dry gas are gradually adjusted according to the coking difficulty of the low-carbon hydrocarbon at high temperature, so that the phenomenon of liquid state or fog drop of the low-carbon hydrocarbon is avoided;
after the gas is input into the superheater, the proportion and the flow of the low-carbon hydrocarbon, the high-temperature steam and/or the gas dry gas are gradually adjusted again according to the working state of the pre-raiser, so that the lifting section of the FCC device works stably;
under the working condition of start-up, the low-carbon hydrocarbon is input into the gasifier for gasification, only high-temperature water vapor and/or dry gas are input into the pre-lifter, after the pre-lifter reaches a preset working state, the low-carbon hydrocarbon is input into the gasifier for gasification, the flow of the low-carbon hydrocarbon gas is gradually increased, and the flow of the high-temperature water vapor and/or the dry gas before and after the low-carbon hydrocarbon gas is input into the superheater is gradually adjusted.
2. The pre-lifting process of an FCC unit as claimed in claim 1, wherein: when the gasifier fails under normal working conditions and needs to be overhauled on line, high-temperature steam and/or dry gas are only input into the pre-lifting device after passing through the heat device, so that the gasifier can be conveniently switched out from the system on line for overhauling, and the gasifier is switched in on line after overhauling.
3. The pre-lifting process of an FCC unit as claimed in claim 1, wherein: when the superheater fails under normal working conditions and needs to be overhauled on line, only high-temperature steam and/or dry gas are input into the pre-raiser, so that the superheater can be cut out from the system on line for overhauling, and the superheater is cut in line after overhauling.
4. The pre-lifting process of an FCC unit as claimed in claim 1, wherein: the gasifier adopts a pressure control mode, the superheater adopts a temperature control mode, and the flow control mode of related input pipelines is combined to realize the accurate control of the pressure, the temperature and the flow of the low-carbon hydrocarbon components.
5. The pre-lifting process of an FCC unit as claimed in claim 1, wherein: and a heat source for heating the gasifier and/or the superheater directly or indirectly comes from a heating furnace, high-temperature water vapor, heat transfer oil, a thermal catalyst or a burning energy of a catalyst regenerator or superheated high-temperature water vapor of an internal heat remover and an external heat remover of the catalyst regenerator.
6. The pre-lifting process of an FCC unit as claimed in claim 1, wherein: the low-carbon hydrocarbon comprises one or more of ethane, propane, isobutane, ethylene-rich gas, normal isobutane, normal isobutene, carbon three, carbon four, carbon five, carbon six, carbon seven, carbon eight and carbon nine; and the lower hydrocarbon comprises one or more components of saturated hydrocarbon, naphthenic hydrocarbon, olefin or aromatic hydrocarbon.
7. A pre-lift system for an FCC unit comprising input lines and valves thereof disposed between a gasifier, a superheater and a pre-lift, characterized in that:
a first input line for inputting low-carbon hydrocarbon to the gasifier is arranged at one side of the gasifier;
a second input pipeline for inputting a gasification state pre-lifting medium to the superheater is arranged between the gasifier and the superheater, and a second front valve is arranged on the second input pipeline;
a third input pipeline for inputting the gasified and superheated pre-lifting medium to the pre-lifter is arranged between the superheater and the pre-lifter, and a third valve is arranged on the third input pipeline;
the second input pipeline is provided with an input pipeline for inputting high-temperature water vapor and/or gas dry gas and a valve thereof;
an input pipeline for inputting high-temperature water vapor and/or gas dry gas and a valve thereof are arranged on the third input pipeline;
along the flowing direction of the gasification state pre-lifting medium, the second front valve, the joint of the input pipeline of the high-temperature water vapor and the second input pipeline, and the joint of the input pipeline of the gas dry gas and the second input pipeline are sequentially positioned on the second input pipeline;
along the flowing direction of the gasified and overheated pre-lifting medium, the third valve, the joint of the input pipeline of the high-temperature water vapor and the third input pipeline, and the joint of the input pipeline of the gas dry gas and the third input pipeline are sequentially positioned on the third input pipeline.
8. The pre-lift system of an FCC unit of claim 7, wherein: and the first input pipeline is provided with a first valve which is used for being matched with a second front valve on a second input pipeline to be independently switched on or switched off the gasifier on line.
9. The pre-lift system of an FCC unit of claim 7, wherein: ninth input pipelines are connected in parallel to two sides of the superheater to replace a seventh input pipeline arranged on the third input pipeline, and a second rear valve is arranged on the second input pipeline and is used for being matched with a third valve to independently cut out or cut out the superheater on line; and a ninth valve is arranged on the ninth input pipeline to replace the seventh valve arranged on the seventh input pipeline;
along the flowing direction of the gasification state pre-lifting medium, a second front valve, the joint of the input pipeline of the high-temperature water vapor and the second input pipeline, the joint of the input pipeline of the gas dry gas and the second input pipeline, the joint of the ninth input pipeline and the second input pipeline, and a second rear valve are sequentially positioned on the second input pipeline;
along the flowing direction of the gasified and overheated pre-lifting medium, the third valve, the joint of the ninth input pipeline and the third input pipeline, the joint of the input pipeline of the high-temperature water vapor and the third input pipeline, and the joint of the input pipeline of the gas dry gas and the third input pipeline are sequentially positioned on the third input pipeline.
10. The pre-lift system of an FCC unit of claim 7, wherein: an eighth input pipeline for inputting high-temperature water vapor is arranged on the third input pipeline to replace a fifth input pipeline arranged on the third input pipeline, and an eighth valve is arranged on the eighth input pipeline to replace a fifth valve arranged on the fifth input pipeline; along the flowing direction of the gasified and overheated state pre-lifting medium, the third valve, the connection part of the seventh input pipeline and the third input pipeline and the connection part of the eighth input pipeline and the third input pipeline are sequentially positioned on the third input pipeline.
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| WO2022109971A1 (en) * | 2020-11-27 | 2022-06-02 | 广州智京科技有限公司 | Pre-lifting system and process of fcc device |
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