CN110591763A - Intelligent enhanced control system and process for coal indirect liquefaction - Google Patents
Intelligent enhanced control system and process for coal indirect liquefaction Download PDFInfo
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- CN110591763A CN110591763A CN201910853203.8A CN201910853203A CN110591763A CN 110591763 A CN110591763 A CN 110591763A CN 201910853203 A CN201910853203 A CN 201910853203A CN 110591763 A CN110591763 A CN 110591763A
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- 239000003245 coal Substances 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000002002 slurry Substances 0.000 claims abstract description 69
- 238000006243 chemical reaction Methods 0.000 claims abstract description 56
- 239000003054 catalyst Substances 0.000 claims abstract description 16
- 239000000047 product Substances 0.000 claims abstract description 15
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 9
- 239000000463 material Substances 0.000 claims description 70
- 239000007791 liquid phase Substances 0.000 claims description 48
- 239000007788 liquid Substances 0.000 claims description 29
- 239000012071 phase Substances 0.000 claims description 28
- 238000000926 separation method Methods 0.000 claims description 15
- 238000012544 monitoring process Methods 0.000 claims description 14
- 230000001276 controlling effect Effects 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 6
- 238000011143 downstream manufacturing Methods 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000012216 screening Methods 0.000 claims description 2
- 230000003416 augmentation Effects 0.000 claims 5
- 230000000694 effects Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 43
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 230000000052 comparative effect Effects 0.000 description 8
- 239000003921 oil Substances 0.000 description 7
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- -1 alkyl olefin Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000007810 chemical reaction solvent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/0035—Periodical feeding or evacuation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
- B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
An intelligent intensified control system and a process for coal indirect liquefaction belong to the technical field of coal indirect liquefaction, wherein a solid-state bed reactor is replaced by a slurry-state bed reactor, and a micro-interface generator is arranged in the reactor, so that crude gas can be better contacted with a catalyst to react, and the product yield is improved; the micro-interface generator is used for smashing the gas, so that the reaction pressure in the slurry bed reactor can be effectively reduced, and the safety of the device is improved; the circulation unit with the function of separating reaction products is arranged outside the slurry bed reactor, so that the structure of the reaction device is simplified, and the reaction efficiency is improved to a certain extent; the invention is also provided with an intelligent control unit to realize the effect of accurately controlling the temperature and the pressure in the slurry bed reactor.
Description
Technical Field
The invention relates to the technical field of coal indirect liquefaction, in particular to an intelligent strengthened control system and process for coal indirect liquefaction.
Background
The indirect coal liquefaction refers to that coal is gasified and purified and then subjected to Fischer-Tropsch synthesis to generate crude products such as gaseous hydrocarbon, liquid hydrocarbon, synthetic wax and the like. The liquid hydrocarbon and the synthetic wax are subjected to hydrotreating to produce products such as diesel oil, gasoline naphtha and refined wax.
Fischer-Tropsch Synthesis (FTS) is a method for indirectly synthesizing oil products from carbonaceous resources such as coal, natural gas, biomass, etc. as raw materials. The product generally comprises heavy oil, light oil, synthetic water (containing organic oxygen-containing compounds such as alcohol, aldehyde, ketone, acid and ester), CO2, methane, lower hydrocarbons (C6 and lower alkyl olefin), unreacted synthesis gas (CO, H2) and nitrogen. The Fischer-Tropsch synthesis tail gas mainly comprises H2, CO, low-carbon hydrocarbon (alkane and olefin below C6), CO2, N2 and the like. The lower hydrocarbon is mainly methane, its content is usually 20% -60% (mol), and it also contains partial C2-C6 olefin, about 1% -10% (mol).
The reactor in the prior indirect coal liquefaction technology mostly adopts a fixed bed reactor for reaction, the catalyst cannot be fully utilized, the reaction efficiency is low, and side reaction is easy to occur; in the reaction process, the influence of various factors on the temperature and the pressure of the reactor is complex, and the traditional control mode cannot well meet the existing accurate control requirement.
Disclosure of Invention
Therefore, the invention provides an intelligent enhanced control system and process for coal indirect liquefaction, which are used for solving the problem of low reaction efficiency of coal indirect liquefaction.
In one aspect, the present invention provides an intelligent enhanced control system for coal indirect liquefaction, comprising: the system comprises a slurry bed reactor, a micro-interface generator, a circulating unit, a separating unit and an intelligent control unit;
the slurry bed reactor is a reaction site for indirect coal liquefaction, and the slurry bed reactor is filled with a product obtained by coal liquefaction and occupies 2/3 of the volume of the whole reactor;
at least one micro-interface generator is arranged in the slurry bed reactor, is connected with an air inlet pipeline and is used for crushing the bubbles of the raw gas into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1 mm;
the circulating unit is connected with a material outlet of the slurry bed reactor and is used for carrying out primary separation and circulating treatment on reaction products;
the separation unit is connected with the circulating unit and is used for separating gas-phase materials and liquid-phase materials from the circulating unit;
the intelligent control unit comprises a sensor, a controller and a cloud processor, the sensor transmits acquired electric signals to the cloud processor, the cloud processor performs screening comparison on reaction parameters returned by the sensor in a cloud database, and sends corresponding commands to the controller after an optimal control method is screened out, so that an optimal control function is realized.
Further, the slurry bed reactor is provided with at least one catalyst additive pipeline.
Furthermore, the slurry bed reactor is provided with a temperature control pipeline, and a heat exchanger is arranged on the pipeline.
Further, the micro-interface generator is a pneumatic generator.
Further, the circulation unit comprises a hot high pressure separator and a circulation pump:
the hot high-pressure separator is used for separating reaction materials from the slurry bed reactor into a gas phase and a liquid phase;
and the circulating pump is used for feeding part of liquid-phase materials obtained by the separation of the hot high-pressure separator back to the slurry bed reactor.
Furthermore, a first baffle and a second baffle which extend upwards from the bottom of the hot high-pressure separator are arranged in the hot high-pressure separator, and the hot high-pressure separator is divided into three parts by the two baffles, wherein the three parts comprise a first part, a middle part and a second part;
the bottom of the first part is connected to the circulating pump through a pipeline and used for conveying materials back to the slurry bed reactor;
the top of the middle part is connected with a material outlet of the tubular reactor through a pipeline and used for recovering the catalyst from the slurry bed reactor;
the bottom of the second part is connected with the hot low-pressure separator through a pipeline and used for conveying materials to the separation unit;
and the top of the hot high-pressure separator is also provided with a gas phase outlet pipeline which can discharge gas into the cold high-pressure separator.
Further, the separation unit includes: a cold high pressure separator, a hot low pressure separator, a cold low pressure separator;
the cold high-pressure separator is used for separating the cooled gas-phase material from the hot high-pressure separator, reducing the pressure of the separated liquid phase and sending the liquid phase to the cold low-pressure separator, and discharging the separated gas to a downstream processing device;
the hot low-pressure separator is used for separating partial liquid-phase materials which are from the hot high-pressure separator and subjected to pressure reduction, sending separated liquid-phase residues to a downstream device, and sending separated gas phases to the cold low-pressure separator after cooling;
a cold low pressure separator for separating material from the cold high pressure separator and the hot low pressure separator to separate product oil.
Further, the sensor includes:
at least one temperature sensor is arranged in the slurry bed reactor and used for monitoring the reaction temperature in the reactor;
at least one pressure sensor is arranged in the slurry bed reactor and used for monitoring the pressure in the reactor;
the at least one first position sensor is arranged at the preset liquid level height of the slurry bed reactor and used for monitoring the height of liquid-phase materials in the reactor;
at least one second position sensor is arranged at the preset liquid level height of the hot high-pressure separator and used for monitoring the height of liquid-phase materials in the separator.
Further, the controller includes:
the first controller is arranged on the heat exchanger and used for controlling the working state of the heat exchanger;
the second controller is arranged on the circulating pump and used for controlling the working state of the circulating pump;
the first control valve is arranged on the air inlet pipeline and used for controlling the air inlet state of the pipeline;
and the second control valve is arranged on the material outlet pipeline of the slurry bed reactor and used for controlling the flow of the material.
In another aspect, the present invention provides an intelligent enhanced control process for coal indirect liquefaction, comprising:
step 1, a micro-interface generator arranged in a slurry bed reactor breaks crude gas from a gas conveying pipeline into micron-sized bubbles, and the micron-sized bubbles of the crude gas are diffused into a liquid phase of the slurry bed reactor through small holes in the micro-interface generator and contact with a catalyst to react;
step 2, enabling the reaction product to enter a circulating unit through a material outlet, separating the reaction product in the circulating unit through a hot high-pressure separator, and enabling the separated gas phase and the other part of liquid phase material to enter a separating unit;
step 3, separating the gas-phase material from the hot high-pressure separator by a cold high-pressure separator in the separation unit, decompressing the separated liquid phase, sending the decompressed liquid phase to a cold low-pressure separator, and discharging the separated gas phase to a downstream processing device;
step 4, the hot low-pressure separator separates partial liquid-phase materials which are from the hot high-pressure separator and subjected to pressure reduction, the separated liquid-phase residues are sent to a downstream device, the separated gas phase is cooled and then sent to the cold low-pressure separator, and the cold low-pressure separator separates the materials from the cold high-pressure separator and the hot low-pressure separator, so that product oil is obtained;
step 5, monitoring the temperature of the reactor by a temperature sensor arranged in the slurry bed reactor, sending an electric signal to a cloud processor by the temperature sensor when the temperature is not matched with a preset value, sending a control command to a first controller by the cloud processor, and realizing a temperature control function by adjusting the power of a heating furnace;
the pressure sensor arranged in the slurry bed reactor monitors the pressure of the reactor, when the pressure is not matched with a preset value, the pressure sensor sends an electric signal to the cloud processor, the cloud processor sends a control command to the first control valve, and the amount of reaction materials entering the reactor is controlled by adjusting the gas flow, so that the control of the reaction rate and the reaction pressure is realized;
the method comprises the following steps that a first position sensor arranged in the slurry bed reactor monitors the liquid level of the reactor, when the liquid level is not matched with a preset value, the first liquid level sensor sends an electric signal to a cloud processor, the cloud processor sends a control command to a second control valve, and the amount of reaction materials flowing out of the reactor is controlled by adjusting the flow;
the setting is in second position sensor in the hot high pressure separator monitors hot high pressure separator's liquid level, and when the liquid level did not match with the default, second position sensor was through sending electric signal to cloud treater, and cloud treater sends control command to the second controller, and the rotational speed through the regulating pump comes the control to flow out hot high pressure separator's reaction material volume.
Compared with the prior art, the invention has the beneficial effects that the traditional fixed bed reactor is changed into the slurry bed reactor, so that gases can be mixed with each other in the reaction bed without pressurization, the contact area of the gases and the catalyst is larger, and the reaction efficiency is improved.
In particular, at least one micro-interface generator is provided in the slurry bed reactor, in which the raw gas is broken up into micro-scale small bubbles having an additional pressure, which are not easily coalesced when they collide with each other, and thus have a larger phase interface area with respect to the gas before breaking up, and thus are more easily reacted under the action of the catalyst.
In particular, the micro-interface generator can break the discharged hydrogen into micron-sized bubbles so as to greatly reduce the air pressure, thereby reducing the reaction pressure in the fluidized bed reactor, saving the energy consumption and ensuring that the whole reaction device is safer.
Furthermore, the hot high-pressure separator of the circulating unit adopts a horizontal tank-shaped design, and the baffle is arranged in the tank-shaped shell, so that catalyst powder and other solid particles can be effectively prevented from entering a circulating pump system, the abrasion to the circulating pump is reduced, and the service life is prolonged.
In particular, the hot high-pressure separator will return a portion of the separated liquid phase product to the slurry bed reactor to ensure that there is sufficient liquid in the reactor to act as a reaction solvent for the raw gas.
Furthermore, an intelligent control unit is arranged in the whole reaction system, so that a worker can know the real-time situation of each data transmitted back by the sensor at any time through mobile equipment, and can realize the accurate control of the height and the temperature of the liquid level in the whole slurry bed reactor in a mode of issuing an instruction or changing an input variable of a target function on site, and the reaction efficiency is further improved.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
FIG. 2 is a control flow chart of an embodiment of the present invention.
Detailed Description
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, it is a schematic structural diagram of an intelligent enhanced control system based on micro-interface coal indirect liquefaction provided by the present invention, and the system includes: the system comprises a slurry bed reactor 1, a micro-interface generator 2, a temperature control pipeline 3, a circulating unit 4, a separating unit 5, an additive adding pipeline 6 and an intelligent control unit 7.
With continued reference to fig. 1, the micro-interface generator 2 is disposed inside the slurry bed reactor 2 to break up the raw gas from the gas pipeline, and the gas is broken up into micro-bubbles of micron level by the micro-interface generator, so that the micro-bubbles are more easily dissolved in the liquid phase to form a gas-liquid emulsion before breaking up, and the contact area with the catalyst is increased, thereby improving the reaction efficiency. At least one catalyst additive pipeline 6 is arranged in the slurry bed reactor 2; the outside of the slurry bed reactor 2 is provided with a temperature control pipeline 3, the pipeline is provided with a heat exchanger 31, and the liquid in the reactor is guided into the temperature control pipeline, so that the heat exchanger is used for heating or cooling the liquid, and the purpose of controlling the temperature is achieved.
With continued reference to fig. 1, the circulation unit 4 includes a hot high pressure separator 41 and a circulation pump 42. Wherein, the hot high-pressure separator 41 is used for separating the reaction material at the top of the slurry bed reactor 2 into a gas phase and a liquid phase, and the circulating pump 42 is used for returning a part of the liquid phase material separated by the hot high-pressure separator 41 to the slurry bed reactor 2 so as to maintain the normal flow of the reaction material in the slurry bed reactor.
Specifically, a first baffle 411 and a second baffle 412 extending upward from the bottom of the hot high-pressure separator 41 are provided in the hot high-pressure separator 41, respectively, so as to divide the hot high-pressure separator 41 into three parts communicating at the upper part (i.e., the first and second baffles 411, 412 do not extend to the top of the hot high-pressure separator 41): an intermediate portion 413 located between the first shutter 411 and the second shutter 412, a first portion 414 located at a side of the first shutter 411, and a second portion 415 located at a side of the second shutter 412. The bottom of the first portion 414 is connected to the circulation pump 42 by a pipe. The top of the middle part 413 is connected to a material outlet at the top of the slurry bed reactor 2 through a pipe. The bottom of the second section 415 is connected to a separation unit 5 via a pipe to separate the desired product. While the top of the hot high-pressure separator 41 is also provided with a gas phase outlet conduit 416. It will be appreciated by those skilled in the art that the hot high pressure separator 41 is a horizontal tank-like separator, although the hot high pressure separator 41 may be other suitable types of separators.
After the material from the slurry bed reactor 2 enters the hot high pressure separator 41, the gas phase material exits from the gas phase outlet pipe 416, and the liquid phase material with the solid catalyst entrained therein first falls into the intermediate portion 413, and then overflows into the first portion 414 and the second portion 415 through the first baffle 411 and the second baffle 412, respectively. At this time, the catalyst particles are mostly deposited in the middle portion 413. The first part 414 sends the overflowed liquid phase material back to the slurry bed reactor 2 and the second part 415 sends the overflowed liquid phase material to the next processing unit.
With continued reference to fig. 1, the separation unit 5 includes: a cold high-pressure separator 51, a hot low-pressure separator 52 and a cold low-pressure separator 53; the cold high-pressure separator 51 separates the gaseous material discharged from the gaseous outlet line 416 of the hot high-pressure separator 41, depressurizes the separated liquid phase and discharges it into the cold low-pressure separator 53, and discharges the separated gaseous phase to a downstream processing unit; the hot low-pressure separator 52 is connected with the second part 415 of the hot high-pressure separator 41, separates partial liquid-phase materials which come from the hot high-pressure separator 41 and are decompressed, sends separated liquid-phase residues to a downstream device, and sends separated gas phases to the cold low-pressure separator 53 after cooling; the cold low-pressure separator 53 is used for separating the materials 52 from the cold high-pressure separator 51 and the hot low-pressure separator to separate out product oil, and the separated oil can enter a downstream rectification system for further treatment.
With continued reference to fig. 1, at least one temperature sensor 72 is disposed within the slurry bed reactor 1 for monitoring the reaction temperature within the reactor; at least one pressure sensor 74 is provided in the slurry bed reactor 1 to monitor the pressure in the reactor; at least one position sensor 73 is arranged at the preset liquid level height of the slurry bed reactor 1 and used for monitoring the height of liquid-phase materials in the reactor; at least one position sensor 76 is arranged at a preset liquid level height of the hot high-pressure separator 41 and used for monitoring the height of liquid-phase materials in the separator; at least one controller is arranged on the heat exchanger 31 and used for controlling the working state of the heat exchanger 31; at least one controller is provided on the circulation pump 42 to control the operating state of the circulation pump; at least one control valve 71 is provided on the intake duct to control the intake state of the duct; at least one control valve 75 is provided on the material outlet pipe of the slurry bed reactor 1 to control the flow rate of the material.
Referring to fig. 1 and fig. 2, the control flow of the present embodiment includes:
step 1, a micro-interface generator arranged in a slurry bed reactor breaks crude gas from a gas conveying pipeline into micron-sized bubbles, and the micron-sized bubbles of the crude gas are diffused into a liquid phase of the slurry bed reactor through small holes in the micro-interface generator and contact with a catalyst to react;
step 2, enabling the reaction product to enter a circulating unit through a material outlet, separating the reaction product in the circulating unit through a hot high-pressure separator, and enabling the separated gas phase and the other part of liquid phase material to enter a separating unit;
step 3, separating the gas phase material from the high-pressure heat separator by a cold high-pressure separator in the separation unit, decompressing the separated liquid phase, sending the decompressed liquid phase to a cold low-pressure separator, and discharging the separated gas phase to a downstream processing device;
step 4, separating partial liquid phase materials which are from the hot high-pressure separator and subjected to pressure reduction by the hot low-pressure separator, sending separated liquid phase residues to a downstream device, cooling separated gas phase and then sending the cooled gas phase to the cold low-pressure separator, and separating the materials from the cold high-pressure separator and the hot low-pressure separator by the cold low-pressure separator to obtain product oil;
step 5, monitoring the temperature of the reactor by a temperature sensor arranged in the slurry bed reactor, sending an electric signal to a cloud processor by the temperature sensor when the temperature is not matched with a preset value, sending a control command to a first controller by the cloud processor, and realizing a temperature control function by adjusting the power of a heating furnace;
the method comprises the following steps that a pressure sensor arranged in a slurry bed reactor monitors the pressure of the reactor, when the pressure is not matched with a preset value, the pressure sensor sends an electric signal to a cloud processor, the cloud processor sends a control command to a first control valve, and the amount of reaction materials entering the reactor is controlled by adjusting the gas flow, so that the control of the reaction rate and the reaction pressure is realized;
the method comprises the following steps that a first position sensor arranged in a slurry bed reactor monitors the liquid level of the reactor, when the liquid level is not matched with a preset value, the first liquid level sensor sends an electric signal to a cloud processor, the cloud processor sends a control command to a second control valve, and the amount of reaction materials flowing out of the reactor is controlled by adjusting the flow;
the second position sensor who sets up in hot high pressure separator monitors hot high pressure separator's liquid level, and when the liquid level did not match with the default, second position sensor was through sending electric signal to cloud treater, and cloud treater sends control command to the second controller, and the rotational speed through the regulating pump comes the control to flow out hot high pressure separator's reaction material volume.
In this embodiment, the pressure sensor is a MIK-P310 pressure sensor manufactured by mike, the temperature sensor is a pt100 temperature sensor manufactured by american control corporation, the position sensor is a CYW11 liquid level transmitter manufactured by stellatellites corporation, and the control valve is an electric control valve manufactured by australian corporation, hiki, jiang.
The operation limiting variables of the present embodiment are shown in table 1:
the reaction conditions and reaction performance of this example are shown in table 2;
TABLE 2
| Temperature (. degree.C.) | 270 |
| Pressure (MPa) | 0.7 |
| Space velocity (ml/g/h) | 18000 |
| Feed gas H2/CO | 1.4 |
| CO conversion (%) | 87.16 |
| CH4(wt％) | 3.08 |
| C2～C4(wt％) | 6.53 |
| C5 +(wt％) | 89.42 |
Comparative example 1
Comparing the above examples, the reactor of this comparative example is a fixed bed reactor, other conditions are unchanged, and the reaction conditions and reaction performance are shown in table 3;
TABLE 3
| Temperature (. degree.C.) | 270 |
| Pressure (MPa) | 1.3 |
| Space velocity (ml/g/h) | 15000 |
| Feed gas H2/CO | 1.8 |
| CO conversion (%) | 73.23 |
| CH4(wt％) | 3.20 |
| C2～C4(wt％) | 8.11 |
| C5 +(wt％) | 88.69 |
Comparative example 2
Comparing the above examples, the reactor of this comparative example is a slurry bed reactor, but the micro-interface generator and the intelligent control unit are not arranged in the reactor, other conditions are not changed, and the reaction conditions and the reaction performance are shown in table 4;
TABLE 4
| Temperature (. degree.C.) | 270 |
| Pressure (MPa) | 2.3 |
| Space velocity (ml/g/h) | 16000 |
| Feed gas H2/CO | 1.5 |
| CO conversion (%) | 78.73 |
| CH4(wt％) | 2.97 |
| C2～C4(wt％) | 7.68 |
| C5 +(wt％) | 90.04 |
The reaction conditions and the reaction performance in the above examples and the three comparative examples were counted, and the statistical results are shown in table 5:
TABLE 5
| Reaction conditions and Properties | Comparative example 1 | Comparative example 2 | Examples |
| Temperature (. degree.C.) | 270 | 270 | 270 |
| Pressure (MPa) | 3 | 2.3 | 0.7 |
| Space velocity (ml/g/h) | 15000 | 16000 | 18000 |
| Feed gas H2/CO | 1.8 | 1.5 | 1.4 |
| CO conversion (%) | 73.23 | 78.73 | 87.16 |
| CH4(wt％) | 3.20 | 2.97 | 3.08 |
| C2～C4(wt％) | 8.11 | 7.68 | 6.53 |
| C5 +(wt％) | 88.69 | 90.04 | 89.42 |
Obviously, the comparison between the above embodiment and the comparative example shows that the slurry bed reactor and the micro-interface generator are applied in the embodiment, and the intelligent control unit and the signal receiving and transmitting unit can adjust the reaction occurrence conditions at any time, so that the gas can fully react under the action of the catalyst, the occurrence of side reactions is reduced, and the product yield is improved; as the gas is broken into micron-level bubbles, the reaction pressure in the slurry bed reactor is reduced, and the safety of the whole device is improved.
Claims (10)
1. An intelligent enhanced control system for coal indirect liquefaction is characterized by comprising: the system comprises a slurry bed reactor, a micro-interface generator, a circulating unit, a separating unit, an intelligent control unit and a signal receiving and transmitting unit;
the slurry bed reactor is a reaction site for indirect coal liquefaction, and the slurry bed reactor is filled with a product obtained by coal liquefaction and occupies 2/3 of the volume of the whole reactor;
at least one micro-interface generator is arranged in the slurry bed reactor, is connected with an air inlet pipeline and is used for crushing the bubbles of the raw gas into micron-sized bubbles with the diameter of more than or equal to 1 mu m and less than 1 mm;
the circulating unit is connected with a material outlet of the slurry bed reactor and is used for carrying out primary separation and circulating treatment on reaction products;
the separation unit is connected with the circulating unit and is used for separating gas-phase materials and liquid-phase materials from the circulating unit;
the intelligent control unit comprises a sensor, a controller and a cloud processor, the sensor transmits acquired electric signals to the cloud processor, the cloud processor performs screening comparison on reaction parameters returned by the sensor in a cloud database, and sends corresponding commands to the controller after an optimal control method is screened out, so that an optimal control function is realized.
2. The intelligent and intensive control system for indirect coal liquefaction of claim 1, wherein the slurry bed reactor is provided with at least one catalyst dosing pipeline.
3. The intelligent and intensive control system for indirect coal liquefaction of claim 1, wherein the slurry bed reactor is provided with a temperature control pipeline, and a heat exchanger is arranged on the pipeline.
4. The intelligent augmentation control system of coal indirect liquefaction of claim 1, wherein the circulation unit comprises a hot high pressure separator and a circulation pump:
the hot high-pressure separator is used for separating reaction materials from the slurry bed reactor into a gas phase and a liquid phase;
and the circulating pump is used for feeding part of liquid-phase materials obtained by the separation of the hot high-pressure separator back to the slurry bed reactor.
5. The intelligent augmentation control system for coal indirect liquefaction according to claim 5, wherein a first baffle and a second baffle extending upwards from the bottom of the hot high-pressure separator are arranged in the hot high-pressure separator, and the two baffles divide the hot high-pressure separator into three parts, including a first part, a middle part and a second part;
the bottom of the first part is connected to the circulating pump through a pipeline and used for conveying materials back to the slurry bed reactor;
the top of the middle part is connected with a material outlet of the tubular reactor through a pipeline and used for recovering the catalyst from the slurry bed reactor;
the bottom of the second part is connected with the hot low-pressure separator through a pipeline and used for conveying materials to the separation unit;
the top of the hot high-pressure separator is also provided with a gas phase outlet pipeline for discharging gas into the cold high-pressure separator.
6. The intelligent augmentation control system of coal indirect liquefaction of claim 1, wherein the separation unit comprises: a cold high pressure separator, a hot low pressure separator, a cold low pressure separator;
the cold high-pressure separator is used for separating the cooled gas-phase material from the hot high-pressure separator, reducing the pressure of the separated liquid phase and sending the liquid phase to the cold low-pressure separator, and discharging the separated gas to a downstream processing device;
the hot low-pressure separator is used for separating partial liquid-phase materials which are from the hot high-pressure separator and subjected to pressure reduction, sending separated liquid-phase residues to a downstream device, and sending separated gas phases to the cold low-pressure separator after cooling;
a cold low pressure separator for separating material from the cold high pressure separator and the hot low pressure separator to separate product oil.
7. The intelligent augmentation control system of coal-indirect liquefaction according to claim 1, wherein the sensor comprises:
at least one temperature sensor is arranged in the slurry bed reactor and used for monitoring the reaction temperature in the reactor;
at least one pressure sensor is arranged in the slurry bed reactor and used for monitoring the pressure in the reactor;
the at least one first position sensor is arranged at the preset liquid level height of the slurry bed reactor and used for monitoring the height of liquid-phase materials in the reactor;
at least one second position sensor is arranged at the preset liquid level height of the hot high-pressure separator and used for monitoring the height of liquid-phase materials in the separator.
8. The intelligent augmentation control system of coal-indirect liquefaction according to claim 1, wherein the controller comprises:
the first controller is arranged on the heat exchanger and used for controlling the working state of the heat exchanger;
the second controller is arranged on the circulating pump and used for controlling the working state of the circulating pump;
the first control valve is arranged on the air inlet pipeline and used for controlling the air inlet state of the pipeline;
and the second control valve is arranged on the material outlet pipeline of the slurry bed reactor and used for controlling the flow of the material.
9. An intelligent intensified control process for coal indirect liquefaction is characterized by comprising the following steps:
step 1, a micro-interface generator arranged in a slurry bed reactor breaks crude gas from a gas conveying pipeline into micron-sized bubbles, and the micron-sized bubbles of the crude gas are diffused into a liquid phase of the slurry bed reactor through small holes in the micro-interface generator and contact with a catalyst to react;
step 2, enabling the reaction product to enter a circulating unit through a material outlet, separating the reaction product in the circulating unit through a hot high-pressure separator, and enabling the separated gas phase and the other part of liquid phase material to enter a separating unit;
step 3, separating the gas-phase material from the hot high-pressure separator by a cold high-pressure separator in the separation unit, decompressing the separated liquid phase, sending the decompressed liquid phase to a cold low-pressure separator, and discharging the separated gas phase to a downstream processing device;
step 4, the hot low-pressure separator separates partial liquid-phase materials which are from the hot high-pressure separator and subjected to pressure reduction, the separated liquid-phase residues are sent to a downstream device, the separated gas phase is cooled and then sent to the cold low-pressure separator, and the cold low-pressure separator separates the materials from the cold high-pressure separator and the hot low-pressure separator, so that product oil is obtained;
step 5, monitoring the temperature of the reactor by a temperature sensor arranged in the slurry bed reactor, sending an electric signal to a cloud processor by the temperature sensor when the temperature is not matched with a preset value, sending a control command to a first controller by the cloud processor, and realizing a temperature control function by adjusting the power of a heating furnace;
the pressure sensor arranged in the slurry bed reactor monitors the pressure of the reactor, when the pressure is not matched with a preset value, the pressure sensor sends an electric signal to the cloud processor, the cloud processor sends a control command to the first control valve, and the amount of reaction materials entering the reactor is controlled by adjusting the gas flow, so that the control of the reaction rate and the reaction pressure is realized;
the method comprises the following steps that a first position sensor arranged in the slurry bed reactor monitors the liquid level of the reactor, when the liquid level is not matched with a preset value, the first liquid level sensor sends an electric signal to a cloud processor, the cloud processor sends a control command to a second control valve, and the amount of reaction materials flowing out of the reactor is controlled by adjusting the flow;
the setting is in second position sensor in the hot high pressure separator monitors hot high pressure separator's liquid level, and when the liquid level did not match with the default, second position sensor was through sending electric signal to cloud treater, and cloud treater sends control command to the second controller, and the rotational speed through the regulating pump comes the control to flow out hot high pressure separator's reaction material volume.
10. The intelligent enhanced control process for coal indirect liquefaction according to claim 9, wherein the reaction pressure is 0.5-2.5 MPa.
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