CN107686747B - Fuel gasification process system capable of improving gas combustion rate - Google Patents
Fuel gasification process system capable of improving gas combustion rate Download PDFInfo
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- CN107686747B CN107686747B CN201710797043.0A CN201710797043A CN107686747B CN 107686747 B CN107686747 B CN 107686747B CN 201710797043 A CN201710797043 A CN 201710797043A CN 107686747 B CN107686747 B CN 107686747B
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- 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
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09D—COATING COMPOSITIONS, e.g. PAINTS, VARNISHES OR LACQUERS; FILLING PASTES; CHEMICAL PAINT OR INK REMOVERS; INKS; CORRECTING FLUIDS; WOODSTAINS; PASTES OR SOLIDS FOR COLOURING OR PRINTING; USE OF MATERIALS THEREFOR
- C09D163/00—Coating compositions based on epoxy resins; Coating compositions based on derivatives of epoxy resins
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09D—COATING COMPOSITIONS, e.g. PAINTS, VARNISHES OR LACQUERS; FILLING PASTES; CHEMICAL PAINT OR INK REMOVERS; INKS; CORRECTING FLUIDS; WOODSTAINS; PASTES OR SOLIDS FOR COLOURING OR PRINTING; USE OF MATERIALS THEREFOR
- C09D183/00—Coating compositions based on macromolecular compounds obtained by reactions forming in the main chain of the macromolecule a linkage containing silicon, with or without sulfur, nitrogen, oxygen, or carbon only; Coating compositions based on derivatives of such polymers
- C09D183/04—Polysiloxanes
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- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09D—COATING COMPOSITIONS, e.g. PAINTS, VARNISHES OR LACQUERS; FILLING PASTES; CHEMICAL PAINT OR INK REMOVERS; INKS; CORRECTING FLUIDS; WOODSTAINS; PASTES OR SOLIDS FOR COLOURING OR PRINTING; USE OF MATERIALS THEREFOR
- C09D5/00—Coating compositions, e.g. paints, varnishes or lacquers, characterised by their physical nature or the effects produced; Filling pastes
- C09D5/08—Anti-corrosive paints
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- 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
- C10J3/74—Construction of shells or jackets
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Abstract
The invention provides a central gas station device for generating gas, which at least comprises: the device comprises a charging pump, a first raw material tank, a second raw material tank, a heating device, a gas generator, a first fan, a second fan, a residual liquid recovery tank and a control cabinet; the feeding pump is connected with the first raw material tank and the second raw material tank through a feeding pipeline; the first raw material tank and the second raw material tank are connected with the gas generator through a feeding pipeline; the heating device is connected with the gas generator through a liquid inlet pipe and a liquid outlet pipe to form a heating loop; the residual liquid recovery tank is connected with a gas generation device through a residual liquid recovery pipeline; the first fan and the second fan are respectively connected with the raw material tank and the residual liquid recovery tank through a first air inlet pipeline; the first fan and the second fan are connected with the gas generator through a second air inlet pipeline.
Description
Technical Field
The invention relates to combustible gas supply equipment, in particular to a gas supply device for gasifying large liquid fuel to generate combustible gas.
Technical Field
A conventional gas generating apparatus generally uses heat of a heater to vaporize a liquid raw material to prepare a gas fuel, and such a vaporizing apparatus often adopts a means of increasing a vaporization temperature in order to improve a vaporization effect; however, the gasification temperature is increased to gasify the liquid raw material, and the liquid raw material itself is thermally decomposed to cause chemical deterioration, so that the generated combustible gas is not only impure and has insufficient calorific value or is exploded and pollutes the environment, but also the gasification device is blocked and stacked, thereby causing great potential safety hazard. Meanwhile, the existing gas generating devices on the market are small-sized factories and are not suitable for large-scale industrial production.
Due to the principle of heat conduction, the conventional heating device loses heat energy in a short time, so that it needs to be heated again in order to ensure the stability of gasification. The invention provides a fuel gasification process system capable of improving the combustion rate of fuel gas, which can stably and intensively produce a large amount of combustible gas without a large amount of heat sources and can produce the gas in a full-automatic, stable and long-term and uninterrupted manner.
Disclosure of Invention
The invention provides a fuel gasification process system capable of improving the combustion rate of fuel gas, which is used for generating fuel gas and at least comprises: the device comprises a charging pump, a first raw material tank, a second raw material tank, a heating device, a gas generator, a first fan, a second fan, a residual liquid recovery tank and a control cabinet;
the feeding pump is connected with the first raw material tank and the second raw material tank through a feeding pipeline; the first raw material tank and the second raw material tank are connected with the gas generator through a feeding pipeline; the heating device is connected with the gas generator through a liquid inlet pipe and a liquid outlet pipe to form a heating loop; the residual liquid recovery tank is connected with a gas generation device through a residual liquid recovery pipeline; the first fan and the second fan are respectively connected with the raw material tank and the residual liquid recovery tank through a first air inlet pipeline; the first fan and the second fan are connected with the gas generator through a second air inlet pipeline;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the first air inlet pipeline is provided with an air inlet pipe first branch, an air inlet pipe second branch and an air inlet pipe third branch, the air inlet pipe first branch is connected with the first raw material tank, the air inlet pipe second branch is connected with the second raw material tank, and the air inlet pipe third branch is connected with the residual liquid recovery tank;
the first feeding pipe branch, the second feeding pipe branch, the first air inlet pipe branch, the second air inlet pipe branch, the third air inlet pipe branch, the second air inlet pipeline and the liquid inlet pipe are all provided with a pressure gauge and an electromagnetic valve;
the top of the gas generator is provided with a gas outlet pipeline; the liquid level meter is arranged on the outer wall of the gas generator and is a side-mounted magnetic turning plate liquid level meter which transmits an electric signal to the control cabinet and judges the liquid level of the fuel tank according to the numerical value of the current.
In one embodiment of the present invention, an anticorrosive layer is provided on the inner tank wall of the first raw material tank and the second raw material tank.
In one embodiment of the present invention, the anticorrosive material of the anticorrosive layer is an epoxy resin-modified silicone resin, and the raw material for the preparation thereof includes: bisphenol a, epoxy resin and silicone monomer;
the preparation method of the anti-corrosion material comprises the following steps:
(1) dissolving allyl bromide (0.9mol), bisphenol A (0.3mol) and potassium carbonate (0.1mol) in acetone (50mL), stirring at room temperature for 30 minutes, heating to 80 ℃, reacting at constant temperature for 12 hours, alternately washing the product with ethanol and water for 3 times, and then drying in a vacuum drying oven at 80 ℃ in vacuum to obtain a polyhydroxy product;
(2) placing the polyhydroxy product (1mol) prepared in the step (1), epichlorohydrin (10mol) and tetramethylammonium bromide (0.06mol) in a four-neck round-bottom flask provided with a magnetic stirrer, a thermometer and a reflux condenser tube, stirring the reactants at room temperature for 15 minutes, heating to 95 ℃ under a nitrogen atmosphere, maintaining for 2 hours, and then dropwise adding a sodium hydroxide solution (2mol,48 wt%) into the four-neck round-bottom flask; maintaining the reaction temperature at 95 ℃ and reacting for 2 hours;
filtering sodium chloride in the reaction process, and carrying out vacuum distillation and separation on the residual epichlorohydrin; then adding a NaOH aqueous solution (1mol, mass fraction: 5%) and toluene into the crude product for further reaction, keeping the reaction at 85 ℃ for 2 hours, then adjusting the pH to 7 by using NaH2PO4 and deionized water, drying by using anhydrous sodium sulfate, and removing residual epoxy chloropropane and solvent by using a rotary evaporator to obtain an epoxy resin monomer;
(3) and (3) taking the epoxy resin monomer and the organic silicon monomer in the step (2) as preparation raw materials (the molar ratio of allyl double bond to SiH is 1: 1.3), adding a Pt catalyst (with the concentration of 20ppm), dissolving in toluene, adding into a four-neck flask, reacting for 2 hours at 90 ℃ in a nitrogen atmosphere, and removing the excess solvent by using a rotary evaporator to obtain the anticorrosive material.
As an embodiment of the present invention, the silicone monomer is 2,4,6, 8-tetramethylcyclotetrasiloxane.
As an embodiment of the present invention, a heating value meter is disposed on the air outlet pipeline.
In one embodiment of the present invention, the outer wall of the gas generator is provided with a heating jacket.
As an embodiment of the invention, an insulating layer is arranged on the outer wall of the heating jacket, and raw materials for preparing an insulating material of the insulating layer comprise, by weight: modified silicon dioxide, dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate,
the preparation method of the modified silicon dioxide comprises the following steps:
1. preparation of silica: adding silicon dioxide and toluene into a flask, heating and dissolving under stirring to prepare a solution, wherein the concentration of the silicon dioxide is 1-25 wt%, cooling to normal temperature, adding polyvinylpyrrolidone and distilled water under stirring, cooling to normal temperature, stirring overnight, extracting the solution from the prepared solution by using an injector, fixing the injector filled with the silicon dioxide solution on a sample rack of electrostatic spinning equipment, connecting a positive electrode of a power supply with an injector needle, connecting a negative electrode of the power supply with a collector, starting a sample injection pump, turning on a high-voltage power supply to carry out electrostatic spinning, turning off the high-voltage power supply, the sample injection pump and the collector after the electrostatic spinning is finished, stopping spinning, and collecting a silicon dioxide crude product; calcining the crude silicon dioxide at high temperature, wherein the calcining temperature is 650 ℃, the temperature rise gradient is 1 ℃ per minute, the calcining time is 5 hours, and the cooling speed is 3 ℃ per minute;
2. dissolving the silica calcined in the step 1 in an ethanol solution, and stirring for 30 minutes under ultrasonic;
3. and (3) reacting the silicon dioxide obtained in the step (2) with polyisocyanate to prepare modified silicon dioxide.
And mixing the modified silicon dioxide obtained by the preparation with dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate, and extruding the mixture by a double-screw extruder to obtain the heat-insulating material.
As an embodiment of the invention, the first raw material tank, the second raw material tank and the residual liquid recovery tank are provided with vent valves and pressure gauges.
In one embodiment of the present invention, the heating medium in the heating device is a superconducting liquid.
As an embodiment of the present invention, the superconducting liquid comprises, by mass: 0.5 to 4 percent of diglycolamine, 0.01 to 0.9 percent of sodium polyphosphate, 0.3 to 0.7 percent of benzotriazole derivative, 0.1 to 0.8 percent of sodium nitrite, 5 to 10 percent of sodium chloride and the balance of water.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1: a schematic of the fuel gasification process system of example 1;
FIG. 2: a schematic view of the structure of the gas generator of example 1.
FIG. 3: a schematic of the fuel gasification process system of example 7;
FIG. 4: a schematic of the fuel gasification process system of example 8;
FIG. 5: a schematic of the fuel gasification process system of example 9;
description of the symbols: the device comprises a feeding pump 1, a first raw material tank 2, a second raw material tank 3, a heating device 4, a gas generator 5, a first fan 6, a second fan 7, a residual liquid recovery tank 8, a control cabinet 9, a feeding pipeline 10, a feeding pipeline 11, a liquid inlet pipe 12, a liquid outlet pipe 13, a residual liquid recovery pipeline 14, a first air inlet pipeline 15, a second air inlet pipeline 16, a pressure gauge 17, an electromagnetic valve 18, an air outlet pipeline 19, a heat value meter 20, a heating sleeve 21, a liquid level meter 22 and an air release valve 23.
A first branch 10-1 of the feed pipe, a second branch 10-2 of the feed pipe, a first branch 11-1 of the feed pipe, and a second branch 11-2 of the feed pipe
A first branch 15-1 of the air inlet pipe, a second branch 15-2 of the air inlet pipe and a third branch 15-3 of the air inlet pipe.
An anti-corrosion layer 24 and an insulating layer 25.
Detailed Description
The disclosure may be understood more readily by reference to the following detailed description of preferred embodiments of the invention and the examples included therein. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. In case of conflict, the present specification, including definitions, will control.
The term "prepared from …" as used herein is synonymous with "comprising". The terms "comprises," "comprising," "includes," "including," "has," "having," "contains," "containing," or any other variation thereof, as used herein, are intended to cover a non-exclusive inclusion. For example, a composition, process, method, article, or apparatus that comprises a list of elements is not necessarily limited to only those elements but may include other elements not expressly listed or inherent to such composition, process, method, article, or apparatus.
The conjunction "consisting of …" excludes any unspecified elements, steps or components. If used in a claim, the phrase is intended to claim as closed, meaning that it does not contain materials other than those described, except for the conventional impurities associated therewith. When the phrase "consisting of …" appears in a clause of the subject matter of the claims rather than immediately after the subject matter, it defines only the elements described in the clause; other elements are not excluded from the claims as a whole.
When an amount, concentration, or other value or parameter is expressed as a range, preferred range, or as a range of upper preferable values and lower preferable values, this is to be understood as specifically disclosing all ranges formed from any pair of any upper range limit or preferred value and any lower range limit or preferred value, regardless of whether ranges are separately disclosed. For example, when a range of "1 to 5" is disclosed, the described range should be interpreted to include the ranges "1 to 4", "1 to 3", "1 to 2 and 4 to 5", "1 to 3 and 5", and the like. When a range of values is described herein, unless otherwise stated, the range is intended to include the endpoints thereof and all integers and fractions within the range.
The singular forms "a", "an" and "the" include plural referents unless the context clearly dictates otherwise. "optional" or "any" means that the subsequently described event or events may or may not occur, and that the description includes instances where the event occurs and instances where it does not.
Approximating language, as used herein throughout the specification and claims, is intended to modify a quantity, such that the invention is not limited to the specific quantity, but includes portions that are literally received for modification without substantial change in the basic function to which the invention is related. Accordingly, the use of "about" to modify a numerical value means that the invention is not limited to the precise value. In some instances, the approximating language may correspond to the precision of an instrument for measuring the value. In the present description and claims, range limitations may be combined and/or interchanged, including all sub-ranges contained therein if not otherwise stated.
In addition, the indefinite articles "a" and "an" preceding an element or component of the invention are not intended to limit the number requirement (i.e., the number of occurrences) of the element or component. Thus, "a" or "an" should be read to include one or at least one, and the singular form of an element or component also includes the plural unless the stated number clearly indicates that the singular form is intended.
"Polymer" means a polymeric compound prepared by polymerizing monomers of the same or different types. The generic term "polymer" embraces the terms "homopolymer", "copolymer", "terpolymer" and "interpolymer".
"interpolymer" means a polymer prepared by polymerizing at least two different monomers. The generic term "interpolymer" includes the term "copolymer" (which is generally used to refer to polymers prepared from two different monomers) and the term "terpolymer" (which is generally used to refer to polymers prepared from three different monomers). It also includes polymers made by polymerizing four or more monomers. "blend" means a polymer formed by two or more polymers being mixed together by physical or chemical means.
The invention provides a fuel gasification process system capable of improving the combustion rate of fuel gas, which is used for generating fuel gas and at least comprises: the device comprises a charging pump, a first raw material tank, a second raw material tank, a heating device, a gas generator, a first fan, a second fan, a residual liquid recovery tank and a control cabinet;
the feeding pump is connected with the first raw material tank and the second raw material tank through a feeding pipeline; the first raw material tank and the second raw material tank are connected with the gas generator through a feeding pipeline; the heating device is connected with the gas generator through a liquid inlet pipe and a liquid outlet pipe to form a heating loop; the residual liquid recovery tank is connected with a gas generation device through a residual liquid recovery pipeline; the first fan and the second fan are respectively connected with the raw material tank and the residual liquid recovery tank through a first air inlet pipeline; the first fan and the second fan are connected with the gas generator through a second air inlet pipeline;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the first air inlet pipeline is provided with an air inlet pipe first branch, an air inlet pipe second branch and an air inlet pipe third branch, the air inlet pipe first branch is connected with the first raw material tank, the air inlet pipe second branch is connected with the second raw material tank, and the air inlet pipe third branch is connected with the residual liquid recovery tank;
the first feeding pipe branch, the second feeding pipe branch, the first air inlet pipe branch, the second air inlet pipe branch, the third air inlet pipe branch, the second air inlet pipeline and the liquid inlet pipe are all provided with a pressure gauge and an electromagnetic valve;
the top of the gas generator is provided with a gas outlet pipeline; the liquid level meter is arranged on the outer wall of the gas generator and is a side-mounted magnetic turning plate liquid level meter which transmits an electric signal to the control cabinet and judges the liquid level of the fuel tank according to the numerical value of the current.
In one embodiment of the present invention, an anticorrosive layer is provided on the inner tank wall of the first raw material tank and the second raw material tank.
In one embodiment of the present invention, the anticorrosive material of the anticorrosive layer is an epoxy resin-modified silicone resin, and the raw material for the preparation thereof includes: bisphenol a, epoxy resin and silicone monomer;
the preparation method of the anti-corrosion material comprises the following steps:
(1) dissolving allyl bromide (0.9mol), bisphenol A (0.3mol) and potassium carbonate (0.1mol) in acetone (50mL), stirring at room temperature for 30 minutes, heating to 80 ℃, reacting at constant temperature for 12 hours, alternately washing the product with ethanol and water for 3 times, and then drying in a vacuum drying oven at 80 ℃ in vacuum to obtain a polyhydroxy product 1;
(2) placing the polyhydroxy product 1(1mol), epichlorohydrin (10mol) and tetramethylammonium bromide (0.06mol) prepared in the step (1) in a four-neck round-bottom flask provided with a magnetic stirrer, a thermometer and a reflux condenser tube, stirring the reactants at room temperature for 15 minutes, heating to 95 ℃ under a nitrogen atmosphere, maintaining for 2 hours, and then dropwise adding a sodium hydroxide solution (2mol,48 wt%) into the four-neck round-bottom flask; maintaining the reaction temperature at 95 ℃ and reacting for 2 hours;
filtering sodium chloride in the reaction process, and carrying out vacuum distillation and separation on the residual epichlorohydrin; then adding a NaOH aqueous solution (1mol, mass fraction: 5%) and toluene into the crude product for further reaction, keeping the reaction at 85 ℃ for 2 hours, then adjusting the pH to 7 by using NaH2PO4 and deionized water, drying by using anhydrous sodium sulfate, and removing residual epoxy chloropropane and solvent by using a rotary evaporator to obtain an epoxy resin monomer;
(3) and (3) taking the epoxy resin monomer and the organic silicon monomer in the step (2) as preparation raw materials (the molar ratio of allyl double bond to SiH is 1: 1.3), adding a Pt catalyst (with the concentration of 20ppm), dissolving in toluene, adding into a four-neck flask, reacting for 2 hours at 90 ℃ in a nitrogen atmosphere, and removing the excess solvent by using a rotary evaporator to obtain the anticorrosive material.
As an embodiment of the present invention, the silicone monomer is 2,4,6, 8-tetramethylcyclotetrasiloxane.
As an embodiment of the present invention, a heating value meter is disposed on the air outlet pipeline.
In one embodiment of the present invention, the outer wall of the gas generator is provided with a heating jacket.
As an embodiment of the invention, an insulating layer is arranged on the outer wall of the heating jacket, and raw materials for preparing an insulating material of the insulating layer comprise, by weight: modified silicon dioxide, dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate,
the preparation method of the modified silicon dioxide comprises the following steps:
1. preparation of silica: adding silicon dioxide and toluene into a flask, heating and dissolving under stirring to prepare a solution, wherein the concentration of the silicon dioxide is 1-25 wt%, cooling to normal temperature, adding polyvinylpyrrolidone and distilled water under stirring, cooling to normal temperature, stirring overnight, extracting the solution from the prepared solution by using an injector, fixing the injector filled with the silicon dioxide solution on a sample rack of electrostatic spinning equipment, connecting a positive electrode of a power supply with an injector needle, connecting a negative electrode of the power supply with a collector, starting a sample injection pump, turning on a high-voltage power supply to carry out electrostatic spinning, turning off the high-voltage power supply, the sample injection pump and the collector after the electrostatic spinning is finished, stopping spinning, and collecting a silicon dioxide crude product; calcining the crude silicon dioxide at high temperature, wherein the calcining temperature is 650 ℃, the temperature rise gradient is 1 ℃ per minute, the calcining time is 5 hours, and the cooling speed is 3 ℃ per minute;
2. dissolving the silica calcined in the step 1 in an ethanol solution, and stirring for 30 minutes under ultrasonic;
3. and (3) reacting the silicon dioxide obtained in the step (2) with polyisocyanate to prepare modified silicon dioxide.
Wherein, in the step 1,
the silica was purchased from Shanghai national drug, LLC of the national drug group.
The spinning of the electrospinning was carried out for 1 day.
The working voltage of the electrostatic spinning is 20 KV.
The spinneret-to-collector distance for the electrospinning was 20 cm.
The push speed of the sample feeding pump is 0.8 ml/h.
The spinneret for electrostatic spinning is a circular single nozzle, so that the modified silicon dioxide prepared by electrostatic spinning is in a fiber structure.
In the step 3, the step of the method is that,
the polyisocyanate is isocyanate group-terminated hyperbranched polyurethane,
the term "isocyanate-terminated hyperbranched polyurethane" refers to a hyperbranched polyurethane terminated with isocyanate groups,
in a preferred embodiment, the method for preparing the isocyanate group-terminated hyperbranched polyurethane at least comprises the following steps:
(1) dissolving isophorone diisocyanate and trimethylolethane in a dimethyl sulfoxide solvent respectively to obtain a diisocyanate solution and a trimethylolethane solution respectively;
(2) at 60 ℃, simultaneously performing nitrogen protection, adding a diisocyanate solution into a trimethylolethane solution, wherein the isocyanate group is excessive, and reacting the reaction system for 10 hours under the condition of heat preservation; heating to 100 ℃, and continuing to react for 12 h;
(3) and after the reaction is finished, carrying out reduced pressure distillation until no solvent exists, dissolving the obtained substance by tetrahydrofuran, settling in methanol, filtering, and carrying out vacuum drying at 80 ℃ for 15h to obtain the isocyanate group terminated hyperbranched polyurethane.
Further, isophorone diisocyanate, 1, 6-hexamethylene diisocyanate, lysine diisocyanate, and isocyanate group-terminated polydimethylsiloxane are all commercially available.
The reaction temperature in the step 3 is 100-: 1.
solvent: the solvent is absolute ethyl alcohol.
And mixing the modified silicon dioxide obtained by the preparation with dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate, and extruding the mixture by a double-screw extruder to obtain the heat-insulating material.
The heat-insulating material is obtained by extruding the mixture through a double-screw extruder and comprises the following specific steps:
the double-screw extruder comprises a feeding system, a double-screw extruder main machine and supercritical CO2Injection system, extrusion die, said feeding system and said supercritical CO2The injection system is sequentially arranged on the main machine of the double-screw extruder, and the extrusion die head is communicated with the outlet of the main machine of the double-screw extruder; the screw of the main machine of the double-screw extruder is formed by arranging and combining a conveying element, a shearing element and a mixing element.
Further, a static mixer is arranged between the outlet of the main machine of the double-screw extruder and the extrusion die head.
Furthermore, a cylinder body of a main machine of the double-screw extruder adopts an electric-oil double-loop temperature control system.
Furthermore, the extrusion die head is provided with die holes which are arranged in a rectangular shape, the aperture is 3mm, the pitch is 5mm, and the length-diameter ratio is 6.
The diameter of a screw of a main machine of the double-screw extruder is 48mm, the length-diameter ratio is 40: 1, and the rotating speed of the screw is 100 r/min.
The raw materials are premixed and dried for 7 hours. According to different electric and oil heating effects, the main machine of the double-screw extruder adopts an electric-oil double-loop temperature control system, and an electric heating system is started firstly and then an oil heating system is carried outAnd (4) a system. The temperature of the double-screw extruder is raised to 250 ℃, and the temperature is kept for 45 min. Through the temperature control of an electric-oil double loop, the mixed and dried material is fed into a main machine of a double-screw extruder by a feeding machine at the speed of 25kg/h, and the material is plasticized through the distance of 16 screw length-diameter ratios. At the position 18 length-diameter ratios of the screws away from the feeding port, the injection gas amount is 80 percent of supercritical CO2The injection pressure is 5.5MPa, (CO)2The pressure of the steel cylinder is 6.5MPa, the steel cylinder is pressurized by a BOOST pressurization system, and the critical state of the steel cylinder is ensured), and meanwhile, the pressure in the extruder is ensured to be 5-6 MPa; under the high pressure of 5-6 MPa, supercritical CO is added2Injecting liquid into a double-screw extruder, wherein a main machine of the double-screw extruder is provided with a small-lead conveying element and a shearing element, so that the semi-molten material forms a compact material seal to prevent gasified CO2Refluxing towards the direction of a feeding port; by shearing of the screw, gasified CO2Dispersed and mixed in the melt. The electric heating system and the heat-conducting oil temperature control system are provided with large-lead conveying elements so as to facilitate the injection of supercritical CO2Has sufficient mixing space; injected CO2Is fully mixed with the material melt at a distance of 14 screw length-diameter ratios and then pushed into a static mixer, and the static mixer is provided with a large number of dispersing and shearing elements such as toothed discs so as to improve the retention time of the material and maximize CO content2CO mixed with the melt and gasified2And further forming a gas-amorphous phase polymer phase-forming system with the melt through a static mixer for further dispersive mixing, and enabling the well-mixed melt to enter a square die head through a transition body. The die head is provided with a small-lead conveying element. As the external pressure is rapidly reduced, the gas dissolved in the melt presents a thermodynamically supersaturated rotating table to instantly form a large number of bubble nuclei, the system is split in phase, the gas continuously diffuses towards the bubble nuclei, the bubbles begin to expand, a large number of bubbles are formed in the heat insulation material, and the continuous foaming extrusion of the heat insulation material is completed.
The modified silicon dioxide, dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate are mixed according to the weight ratio of 10: 0.1: 30: 30: 15.
as an embodiment of the invention, the first raw material tank, the second raw material tank and the residual liquid recovery tank are provided with vent valves and pressure gauges.
In one embodiment of the present invention, the heating medium in the heating device is a superconducting liquid.
As an embodiment of the present invention, the superconducting liquid comprises, by mass: 0.5 to 4 percent of diglycolamine, 0.01 to 0.9 percent of sodium polyphosphate, 0.3 to 0.7 percent of benzotriazole derivative, 0.1 to 0.8 percent of sodium nitrite, 5 to 10 percent of sodium chloride and the balance of water.
Diglycolamine: has a chemical formula of C4H11NO2CAS number 929-06-6, purchased from Shanghai Demaol chemical Co., Ltd.
Sodium polyphosphate: the sodium polyphosphate is prepared from sodium dipolyphosphate and sodium tripolyphosphate according to the weight ratio of 1: 2, or a mixture thereof.
The sodium dimeric phosphate and the sodium tripolyphosphate are purchased from Shanghai Limited company of the national drug group.
Benzotriazole derivatives: the benzotriazole derivative is dimethyl benzotriazole, specifically 5, 7-dimethyl-1H-benzotriazole, has a CAS number of 49636-63-7, and is purchased from Arch Bioscience Company.
The preparation method of the superconducting liquid comprises the following steps:
a. weighing diglycolamine, sodium nitrite, sodium chloride and water according to the component proportion of the superconducting liquid, stirring and mixing at the temperature of 20-25 ℃, and controlling the stirring speed to be more than 500 revolutions per minute;
b. standing and precipitating the stirred materials in the step a, and then stirring again until the materials are uniformly mixed for later use;
c. b, sequentially adding the rest components into the material obtained in the step b in no sequence, adding another component after each component is added, stirring and uniformly mixing until the last component is added, and uniformly mixing to obtain superconducting liquid;
d. and c, hermetically storing the superconducting fluid obtained in the step c in a refrigeration house.
In the invention, the temperature of the superconducting liquid is raised to a proper temperature by an electric heating mode.
In the invention, a thermometer is arranged on the heating device.
In another aspect of the present invention, a process flow of a fuel gasification process system capable of increasing a combustion rate of a fuel gas is provided: liquefied fuel enters into first head tank through the first branch of filling tube on the charge pump through the charging conduit, enters into the second head tank through the second branch of filling tube, during first head tank and second head tank were squeezed into with gas respectively to first head tank and second head tank through the first branch of intake pipe and intake pipe second branch on the first intake duct of first fan and second fan, the gas of squeezing into produced pressure and enters into gas generator through the first branch of inlet pipe and inlet pipe second branch respectively with liquefied fuel in first head tank and the second head tank. The superconducting liquid in the heating device enters the heating sleeve through the liquid inlet pipe to heat the liquefied fuel in the gas generator, and then flows back into the heating device through the liquid outlet pipe. The first fan and the second fan drive gas into the gas generator through the second gas inlet pipe and penetrate into the bottom of the generator, so that the gasification of liquid fuel is promoted; the gasified liquid fuel is conveyed out through the air outlet pipeline for use.
The outer wall of the gas generator is provided with a side-mounted magnetic turning plate liquid level meter for monitoring the liquid level of liquid fuel in the gas generator, 4-20 mA current can be fed back by the liquid level meter when the liquid level is different, and the liquid level position can be known according to the current value. The upper and lower levels are the upper and lower level limits we have set. When the liquid level is lower than the lower limit of the liquid level, the control cabinet can control the amount of gas transmitted by the fan, open the electromagnetic valve on the feeding pipeline and increase the content of liquid fuel entering the gas generator; when the liquid level is higher than the upper limit of the liquid level, the control cabinet closes the electromagnetic valve on the feeding pipeline to stop adding the liquid fuel.
And a heat value meter is arranged on the gas outlet pipeline and used for monitoring the heat value of the gas to be output and ensuring the stability of the heat value of the gas.
When the heat value is lower than the lower limit of the set value, the liquid level and the heating temperature of the gasifier can be increased, and the gasification speed of the liquid fuel is increased; when the heat value is higher than the upper limit of the set value, the liquid level and the heating temperature of the gasifier are reduced, and the gasification speed of the liquid fuel is slowed down.
The liquid level department of gas generator is provided with the liquid outlet, the liquid outlet passes through the raffinate recovery pipeline and is connected with the raffinate recovery jar, and when the calorific value of waiting to export gas was very low all the time, opened the solenoid valve on the raffinate recovery pipeline, retrieved the raffinate in the raffinate recovery jar.
All be provided with atmospheric valve and manometer on first head tank, second head tank and the raffinate recovery tank, when the gas of inputing first head tank, second head tank and raffinate recovery tank was too much, some pressures of release can be followed to the atmospheric valve, prevent to burst.
Preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings.
Example 1: the present embodiment provides a fuel gasification process system capable of increasing a gas combustion rate, for generating a gas, the fuel gasification process system capable of increasing the gas combustion rate at least comprises: the device comprises a charging pump 1, a first raw material tank 2, a second raw material tank 3, a heating device 4, a gas generator 5, a first fan 6, a second fan 7, a residual liquid recovery tank 8 and a control cabinet 9;
the feeding pump 1 is connected with the first raw material tank 2 and the second raw material tank 3 through a feeding pipeline 10; the first raw material tank 2 and the second raw material tank 3 are connected with a gas generator 5 through a feeding pipeline 11; the heating device 4 is connected with the gas generator 5 through a liquid inlet pipe 12 and a liquid outlet pipe 13 to form a heating loop; the residual liquid recovery tank 8 is connected with the gas generator 5 through a residual liquid recovery pipeline 14; the first fan 6 and the second fan 7 are respectively connected with the first raw material tank 2, the second raw material tank 3 and the residual liquid recovery tank 8 through a first air inlet pipeline 15; the first fan 6 and the second fan 7 are connected with the gas generator 5 through a second gas inlet pipeline 16;
the feeding pipeline 10 is provided with a first feeding pipe branch 10-1 and a second feeding pipe branch 10-2, the first feeding pipe branch 10-1 is connected with the first raw material tank 2, and the second feeding pipe branch 10-2 is connected with the second raw material tank 3;
the feeding pipeline 11 is provided with a first feeding pipe branch 11-1 and a second feeding pipe branch 11-2, the first feeding pipe branch 11-1 is connected with the first raw material tank 2, and the second feeding pipe branch 11-2 is connected with the second raw material tank 3;
the first air inlet pipeline 15 is provided with an air inlet pipe first branch 15-1, an air inlet pipe second branch 15-2 and an air inlet pipe third branch 15-3, the air inlet pipe first branch 15-1 is connected with the first raw material tank 2, the air inlet pipe second branch 15-2 is connected with the second raw material tank 3, and the air inlet pipe third branch 15-3 is connected with the residual liquid recovery tank 8;
the first feeding pipe branch 10-1, the second feeding pipe branch 10-2, the first feeding pipe branch 11-1, the second feeding pipe branch 11-2, the first air inlet pipe branch 15-1, the second air inlet pipe branch 15-2, the third air inlet pipe branch 15-3, the second air inlet pipeline 16 and the liquid inlet pipe 12 are all provided with a pressure gauge 17 and an electromagnetic valve 18;
the top of the gas generator 5 is provided with a gas outlet pipe 19.
A heat value meter 20 is arranged on the air outlet pipeline 19.
The outer wall of the gas generator 5 is provided with a heating jacket 21.
A liquid level meter 22 is arranged on the outer wall of the gas generator 5.
And the first raw material tank 2, the second raw material tank 3 and the residual liquid recovery tank 8 are all provided with an emptying valve 23 and a pressure gauge 17.
The control cabinet 9 is used for controlling the pressure gauge 17 and the electromagnetic valve 18 on the first feeding pipe branch 10-1, the second feeding pipe branch 10-2, the first feeding pipe branch 11-1, the second feeding pipe branch 11-2, the first air inlet pipe branch 15-1, the second air inlet pipe branch 15-2, the third air inlet pipe branch 15-3, the second air inlet pipe 16 and the liquid inlet pipe 12.
An anti-corrosion layer is arranged on the inner walls of the first raw material tank and the second raw material tank, an anti-corrosion material of the anti-corrosion layer is epoxy resin modified organic silicon resin, and the preparation raw materials comprise: bisphenol a, epoxy resin and silicone monomer;
the preparation method of the anti-corrosion material comprises the following steps:
(1) dissolving 0.9mol of allyl bromide, 0.3mol of bisphenol A and 0.1mol of potassium carbonate in 50mL of acetone, stirring at room temperature for 30 minutes, heating to 80 ℃, reacting at constant temperature for 12 hours, alternately washing the product with ethanol and water for 3 times, and then drying in a vacuum drying oven at 80 ℃ in vacuum to obtain a polyhydroxy product;
(2) placing 1mol of polyhydroxy product, 10mol of epichlorohydrin and 0.06mol of tetramethylammonium bromide obtained in the step (1) into a four-neck round-bottom flask provided with a magnetic stirrer, a thermometer and a reflux condenser tube, stirring reactants at room temperature for 15 minutes, heating to 95 ℃ under nitrogen atmosphere, maintaining for 2 hours, and then dropwise adding 2mol of 48 wt% sodium hydroxide solution into the four-neck round-bottom flask; maintaining the reaction temperature at 95 ℃ and reacting for 2 hours;
filtering sodium chloride in the reaction process, and carrying out vacuum distillation and separation on the residual epichlorohydrin; then 1mol of the mixture is used, and the mass fraction is as follows: adding 5% NaOH aqueous solution and toluene into the crude product for further reaction, keeping the reaction at 85 ℃, adjusting the pH to 7 by using NaH2PO4 and deionized water after 2 hours, drying by using anhydrous sodium sulfate, and removing residual epoxy chloropropane and solvent by using a rotary evaporator to obtain an epoxy resin monomer;
(3) and (3) taking the epoxy resin monomer and the organic silicon monomer in the step (2) as preparation raw materials, adding a Pt catalyst, dissolving in toluene, adding into a four-neck flask, reacting for 2 hours at 90 ℃ in a nitrogen atmosphere, and removing excess solvent by using a rotary evaporator to obtain the anticorrosive material.
The organosilicon monomer is 2,4,6, 8-tetramethylcyclotetrasiloxane.
The preparation method of the modified silicon dioxide comprises the following steps:
1. preparation of silica: adding silicon dioxide and toluene into a flask, heating and dissolving under stirring to prepare a solution, wherein the concentration of the silicon dioxide is 15 wt%, cooling to normal temperature, adding polyvinylpyrrolidone and distilled water under stirring, cooling to normal temperature, stirring overnight, extracting the solution from the prepared solution by using an injector, fixing the injector filled with the silicon dioxide solution on a sample rack of electrostatic spinning equipment, connecting a power supply anode with an injector needle, connecting a power supply cathode with a collector, starting a sample injection pump, turning on a high-voltage power supply to carry out electrostatic spinning, turning off the high-voltage power supply, the sample injection pump and the collector after the electrostatic spinning is finished, stopping spinning, and collecting a silicon dioxide crude product; calcining the crude silicon dioxide at high temperature, wherein the calcining temperature is 650 ℃, the temperature rise gradient is 1 ℃ per minute, the calcining time is 5 hours, and the cooling speed is 3 ℃ per minute;
2. dissolving the silica calcined in the step 1 in an ethanol solution, and stirring for 30 minutes under ultrasonic;
3. and (3) reacting the silicon dioxide obtained in the step (2) with polyisocyanate to prepare modified silicon dioxide.
Wherein, in the step 1,
the silica was purchased from Shanghai Limited liability company, national drug group.
The spinning of the electrospinning was carried out for 1 day.
The working voltage of the electrostatic spinning is 20 KV.
The spinneret-to-collector distance for the electrospinning was 20 cm.
The push speed of the sample feeding pump is 0.8 ml/h.
The spinneret for electrostatic spinning is a circular single nozzle, so that the modified silicon dioxide prepared by electrostatic spinning is in a fiber structure.
In the step 3, the step of the method is that,
the polyisocyanate is isocyanate group-terminated hyperbranched polyurethane,
the term "isocyanate-terminated hyperbranched polyurethane" refers to a hyperbranched polyurethane terminated with isocyanate groups,
in a preferred embodiment, the method for preparing the isocyanate group-terminated hyperbranched polyurethane at least comprises the following steps:
(1) dissolving isophorone diisocyanate and trimethylolethane in a dimethyl sulfoxide solvent respectively to obtain a diisocyanate solution and a trimethylolethane solution respectively;
(2) at 60 ℃, simultaneously performing nitrogen protection, adding a diisocyanate solution into a trimethylolethane solution, wherein the isocyanate group is excessive, and reacting the reaction system for 10 hours under the condition of heat preservation; heating to 100 ℃, and continuing to react for 12 h;
(3) and after the reaction is finished, carrying out reduced pressure distillation until no solvent exists, dissolving the obtained substance by tetrahydrofuran, settling in methanol, filtering, and carrying out vacuum drying at 80 ℃ for 15h to obtain the isocyanate group terminated hyperbranched polyurethane.
Further, isophorone diisocyanate, 1, 6-hexamethylene diisocyanate, lysine diisocyanate, and isocyanate group-terminated polydimethylsiloxane are all commercially available.
The reaction temperature of the step 3 is 110 ℃, the reaction time is 4h, and the weight ratio of the polyisocyanate to the modified polyethylene is 7: 1.
and mixing the modified silicon dioxide obtained by the preparation with dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate, and extruding the mixture by a double-screw extruder to obtain the heat-insulating material.
The heat-insulating material is obtained by extruding the mixture through a double-screw extruder and comprises the following specific steps:
the double-screw extruder comprises a feeding system, a double-screw extruder main machine and supercritical CO2Injection system, extrusion die, said feeding system and said supercritical CO2The injection system is sequentially arranged on the main machine of the double-screw extruder, and the extrusion die head is communicated with the outlet of the main machine of the double-screw extruder; the screw of the main machine of the double-screw extruder is formed by arranging and combining a conveying element, a shearing element and a mixing element.
Further, a static mixer is arranged between the outlet of the main machine of the double-screw extruder and the extrusion die head.
Furthermore, a cylinder body of a main machine of the double-screw extruder adopts an electric-oil double-loop temperature control system.
Furthermore, the extrusion die head is provided with die holes which are arranged in a rectangular shape, the aperture is 3mm, the pitch is 5mm, and the length-diameter ratio is 6.
The diameter of a screw of a main machine of the double-screw extruder is 48mm, the length-diameter ratio is 40: 1, and the rotating speed of the screw is 100 r/min.
The raw materials are premixed and dried for 7 hours. According to different electric and oil heating effects, the main machine of the double-screw extruder adopts an electric-oil double-loop temperature control system, and an electric heating system is started first and then an oil heating system is started. The temperature of the double-screw extruder is raised to 250 ℃, and the temperature is kept for 45 min. Through the temperature control of an electric-oil double loop, the mixed and dried material is fed into a main machine of a double-screw extruder by a feeding machine at the speed of 25kg/h, and the material is plasticized through the distance of 16 screw length-diameter ratios. At the position 18 length-diameter ratios of the screws away from the feeding port, the injection gas amount is 80 percent of supercritical CO2The injection pressure is 5.5MPa, (CO)2The pressure of the steel cylinder is 6.5MPa, the steel cylinder is pressurized by a BOOST pressurization system, and the critical state of the steel cylinder is ensured), and meanwhile, the pressure in the extruder is ensured to be 5-6 MPa; under the high pressure of 5-6 MPa, supercritical CO is added2Injecting liquid into a double-screw extruder, wherein a main machine of the double-screw extruder is provided with a small-lead conveying element and a shearing element, so that the semi-molten material forms a compact material seal to prevent gasified CO2Refluxing towards the direction of a feeding port; by shearing of the screw, gasified CO2Dispersed and mixed in the melt. The electric heating system and the heat-conducting oil temperature control system are provided with large-lead conveying elements so as to facilitate the injection of supercritical CO2Has sufficient mixing space; injected CO2Is fully mixed with the material melt at a distance of 14 screw length-diameter ratios and then pushed into a static mixer, and the static mixer is provided with a large number of dispersing and shearing elements such as toothed discs so as to improve the retention time of the material and maximize CO content2CO mixed with the melt and gasified2And further forming a gas-amorphous phase polymer phase-forming system with the melt through a static mixer for further dispersive mixing, and enabling the well-mixed melt to enter a square die head through a transition body. The die head is provided with a small-lead conveying element. As the external pressure is rapidly reduced, the gas dissolved in the melt presents a thermodynamically supersaturated rotating table to instantly form a large number of bubble nuclei, the system is split in phase, the gas continuously diffuses towards the bubble nuclei, the bubbles begin to expand, a large number of bubbles are formed in the heat insulation material, and the continuous foaming extrusion of the heat insulation material is completed.
The modified silicon dioxide, dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate are mixed according to the weight ratio of 10: 0.1: 30: 30: 15.
the heating medium in the heating device 4 is superconducting liquid, and the superconducting liquid comprises the following raw materials in percentage by mass: 1.2% of diglycolamine, 0.3% of sodium polyphosphate, 0.5% of benzotriazole derivative, 0.3% of sodium nitrite, 6% of sodium chloride and the balance of water.
Diglycolamine: has a chemical formula of C4H11NO2CAS number 929-06-6, purchased from Shanghai Demaol chemical Co., Ltd.
Sodium polyphosphate: the sodium polyphosphate is prepared from sodium dipolyphosphate and sodium tripolyphosphate according to the weight ratio of 1: 2, or a mixture thereof.
The sodium dimeric phosphate and the sodium tripolyphosphate are purchased from Shanghai Limited company of the national drug group.
Benzotriazole derivatives: the benzotriazole derivative of this example was 5, 7-dimethyl-1H-benzotriazole with a CAS number of 49636-63-7, available from Arch Bioscience Company.
The preparation method of the superconducting liquid comprises the following steps:
a. weighing diglycolamine, sodium nitrite, sodium chloride and water according to the component proportion of the superconducting liquid, stirring and mixing at the temperature of 20-25 ℃, and controlling the stirring speed to be more than 500 revolutions per minute;
b. standing and precipitating the stirred materials in the step a, and then stirring again until the materials are uniformly mixed for later use;
c. b, sequentially adding the rest components into the material obtained in the step b in no sequence, adding another component after each component is added, stirring and uniformly mixing until the last component is added, and uniformly mixing to obtain superconducting liquid;
d. and c, hermetically storing the superconducting fluid obtained in the step c in a refrigeration house.
In this embodiment, the temperature of the superconducting liquid is raised to a suitable temperature by electrical heating.
In this embodiment, the heating device is provided with a thermometer.
In another aspect of this embodiment, a process flow for generating gas by the central gas station device is provided: the liquefied fuel enters the first raw material tank 2 through the feeding pump 1 through the first feeding pipe branch 10-1 on the feeding pipeline 10 and enters the second raw material tank 3 through the second feeding pipe branch 10-2, the first fan 6 and the second fan 7 respectively pump gas into the first raw material tank 2 and the second raw material tank 3 through the first air inlet pipe branch 15-1 and the second air inlet pipe branch 15-2 on the first air inlet pipeline 15, and the pumped gas generates pressure to enable the liquefied fuel in the first raw material tank 2 and the second raw material tank 3 to respectively enter the gas generator 5 through the first feeding pipe branch 11-1 and the second feeding pipe branch 11-2. The superconducting liquid in the heating device 4 enters the heating jacket 21 through the liquid inlet pipe 12 to heat the liquefied fuel in the gas generator 5, and then returns to the heating device 4 through the liquid outlet pipe 12. The first fan 6 and the second fan 7 drive gas into the gas generator 5 through the second gas inlet pipeline 16 to reach the bottom of the gas generator so as to promote the gasification of the liquid fuel; the gasified liquid fuel is delivered out through the air outlet pipeline 19 for use.
The outer wall of the gas generator is provided with a side-mounted magnetic turning plate liquid level meter for monitoring the liquid level of liquid fuel in the gas generator, 4-20 mA current can be fed back by the liquid level meter when the liquid level is different, and the liquid level position can be known according to the current value. The upper and lower levels are the upper and lower level limits we have set. When the liquid level is lower than the lower limit of the liquid level, the control cabinet can control the amount of gas transmitted by the fan, open the electromagnetic valve on the feeding pipeline and increase the content of liquid fuel entering the gas generator; when the liquid level is higher than the upper limit of the liquid level, the control cabinet closes the electromagnetic valve on the feeding pipeline to stop adding the liquid fuel.
And a heat value meter is arranged on the gas outlet pipeline and used for monitoring the heat value of the gas to be output and ensuring the stability of the heat value of the gas.
When the heat value is lower than the lower limit of the set value, the liquid level and the heating temperature of the gasifier can be increased, and the gasification speed of the liquid fuel is increased; when the heat value is higher than the upper limit of the set value, the liquid level and the heating temperature of the gasifier are reduced, and the gasification speed of the liquid fuel is slowed down.
A liquid outlet is arranged at the liquid level of the fuel in the gas generator 5, the liquid outlet is connected with a residual liquid recovery tank 8 through a residual liquid recovery pipeline 14, when the calorific value of the gasified fuel gas to be output is low all the time, an electromagnetic valve 18 on the residual liquid recovery pipeline 14 is opened, and the residual liquid is recovered into the residual liquid recovery tank 8.
All be provided with atmospheric valve 23 and manometer 17 on first head tank 2, second head tank 3 and the raffinate recovery tank 8, when the gas of inputing first head tank 2, second head tank 3 and raffinate recovery tank 8 was too much, can follow atmospheric valve 23 and release some pressure, prevent to burst.
Example 2: the difference from example 1 is that the inner wall of the raw material tank is free of an anti-corrosion layer.
Example 3: the difference from example 1 is that 2,4,6, 8-tetramethylcyclotetrasiloxane is replaced by 1,1,2, 2-tetramethyldisilane in the preparation of the corrosion protection.
Example 4: the difference from the embodiment 1 is that the outer wall of the heating jacket is free of insulation.
Example 5: the difference from example 1 is that the modified silica was replaced with commercially available silica, which was purchased from Shanghai Aladdin Biotech, Inc., in the raw material for the insulation layer.
Example 6: the difference from example 1 is that the benzotriazole derivative is 6, 7-dimethyl-1H-benzotriazole with CAS number 35899-34-4, available from Arch Bioscience Company.
Example 7: the difference from example 1 is that the fuel gasification process system has only one feed tank, the first feed tank.
In this embodiment, the same reference numerals are used for the same components as in embodiment 1, and detailed description is omitted, and only different components will be described in detail.
The pipes connected to the first head tank are all removed.
Example 8: the difference from the embodiment 1 is that the fuel gasification process system only has one fan, namely a first fan.
The pipes connected with the first fan are all removed.
In this embodiment, the same reference numerals are used for the same components as in embodiment 1, and detailed description is omitted, and only different components will be described in detail.
Example 9: the difference from example 1 is that the central gas station unit has no raffinate recovery tank.
In this embodiment, the same reference numerals are used for the same components as in embodiment 1, and detailed description is omitted, and only different components will be described in detail.
The pipes connected with the raffinate recovery tank are all removed.
Example 10: the difference from the embodiment 1 is that in the fuel gasification process system, the inner wall of the raw material tank is not provided with an anti-corrosion layer, and the outer wall of the heating jacket is not provided with an insulating layer.
1. The following tests were carried out for examples 1 to 10:
testing the calorific value of the fuel-gasified gas conveyed from the gas outlet pipeline and the stability of the calorific value:
the above calorific value is given in Kcal. The stability test means that the calorific value of the gas discharged from the gas outlet pipe was measured 30 minutes after the start of the operation of the central gas station. The first data to be tested after the start of the operation for 30 minutes was "heat value at 0 second", the second data to be tested after the start of the operation for 30 minutes and 30 seconds was "heat value at 30 seconds", and so on.
2. And (3) testing the corrosion resistance:
the liquid inlet pipe (or liquid outlet pipe) in examples 1 to 8 was placed in a chlorine dioxide aqueous solution (concentration: 50ppm) to perform a corrosion performance test.
A level: the surface is smooth, has no spots and rust;
b stage: the surface is not smooth, has spots and is not rusted;
c level: the surface was not smooth, speckled, rusted.
3. Testing the heat preservation performance:
after heating tap water to 80 ℃, the tap water was placed in a sealed container prepared from the liquid inlet pipe (or liquid outlet pipe) of examples 1 to 8 and a sealed container prepared from carbon steel for 24 hours, respectively, and the temperature after 24 hours was measured.
And (3) testing results:
wherein the room temperature is 25-28 ℃.
4. Heating test: 500ml of the superconducting fluids of examples 1 and 6 were put in a 500ml glass beaker, and a heating test was conducted simultaneously using the same 900W electric furnace to measure the time for heating to 70 ℃.
5. The superconducting fluids of examples 1 and 6 were used to determine their thermal conductivities at 30 ℃.
Claims (5)
1. A fuel gasification process system for producing a fuel gas, the fuel gasification process system capable of increasing a combustion rate of the fuel gas, the fuel gasification process system comprising: the device comprises a charging pump, a first raw material tank, a second raw material tank, a heating device, a gas generator, a first fan, a second fan, a residual liquid recovery tank and a control cabinet;
the feeding pump is connected with the first raw material tank and the second raw material tank through a feeding pipeline; the first raw material tank and the second raw material tank are connected with the gas generator through a feeding pipeline; the heating device is connected with the gas generator through a liquid inlet pipe and a liquid outlet pipe to form a heating loop; the residual liquid recovery tank is connected with a gas generation device through a residual liquid recovery pipeline;
the first fan and the second fan are respectively connected with the raw material tank and the residual liquid recovery tank through a first air inlet pipeline; the first fan and the second fan are connected with the gas generator through a second air inlet pipeline;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the feeding pipeline is provided with a first feeding pipe branch and a second feeding pipe branch, the first feeding pipe branch is connected with the first raw material tank, and the second feeding pipe branch is connected with the second raw material tank;
the first air inlet pipeline is provided with an air inlet pipe first branch, an air inlet pipe second branch and an air inlet pipe third branch, the air inlet pipe first branch is connected with the first raw material tank, the air inlet pipe second branch is connected with the second raw material tank, and the air inlet pipe third branch is connected with the residual liquid recovery tank;
the first feeding pipe branch, the second feeding pipe branch, the first air inlet pipe branch, the second air inlet pipe branch, the third air inlet pipe branch, the second air inlet pipeline and the liquid inlet pipe are all provided with a pressure gauge and an electromagnetic valve;
the top of the gas generator is provided with a gas outlet pipeline; a liquid level meter is arranged on the outer wall of the gas generator, the liquid level meter is a side-mounted magnetic turning plate liquid level meter, the side-mounted magnetic turning plate liquid level meter transmits an electric signal to the control cabinet, and the liquid level of the fuel tank is judged according to the numerical value of the current;
the inner walls of the first raw material tank and the second raw material tank are provided with anti-corrosion layers;
the anticorrosion material of the anticorrosion layer is epoxy resin modified organic silicon resin, and the preparation raw materials comprise: bisphenol a, epoxy resin and silicone monomer;
the preparation method of the anti-corrosion material comprises the following steps:
(1) dissolving 0.9mol of allyl bromide, 0.3mol of bisphenol A and 0.1mol of potassium carbonate in 50mL of acetone, stirring at room temperature for 30 minutes, heating to 80 ℃, reacting at constant temperature for 12 hours, alternately washing the product with ethanol and water for 3 times, and then drying in a vacuum drying oven at 80 ℃ in vacuum to obtain a polyhydroxy product;
(2) placing 1mol of polyhydroxy product, 10mol of epichlorohydrin and 0.06mol of tetramethylammonium bromide obtained in the step (1) into a four-neck round-bottom flask provided with a magnetic stirrer, a thermometer and a reflux condenser tube, stirring reactants at room temperature for 15 minutes, heating to 95 ℃ under nitrogen atmosphere, maintaining for 2 hours, and then dropwise adding 2mol of 48 wt% sodium hydroxide solution into the four-neck round-bottom flask; maintaining the reaction temperature at 95 ℃ and reacting for 2 hours;
filtering sodium chloride in the reaction process, and carrying out vacuum distillation and separation on the residual epichlorohydrin; then 1mol of the mixture is used, and the mass fraction is as follows: adding 5% NaOH water solution and toluene into the crude product for further reaction, keeping the reaction at 85 ℃ for 2 hours, and then using NaH2PO4Adjusting the pH value to 7 with deionized water, drying with anhydrous sodium sulfate, and removing residual epoxy chloropropane and solvent with a rotary evaporator to obtain an epoxy resin monomer;
(3) taking the epoxy resin monomer and the organic silicon monomer in the step (2) as preparation raw materials, adding a Pt catalyst, dissolving in toluene, adding into a four-neck flask, reacting for 2 hours at 90 ℃ in a nitrogen atmosphere, and removing excess solvent by using a rotary evaporator to obtain the anticorrosive material;
the organosilicon monomer is 2,4,6, 8-tetramethylcyclotetrasiloxane;
the outer wall of the gas generator is provided with a heating sleeve;
the outer wall of heating jacket is provided with the heat preservation, the insulation material's of heat preservation preparation raw materials contains by weight: modified silicon dioxide, dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate,
the preparation method of the modified silicon dioxide comprises the following steps:
1) and preparing silicon dioxide: adding silicon dioxide and toluene into a flask, heating and dissolving under stirring to prepare a solution, wherein the concentration of the silicon dioxide is 1-25 wt%, cooling to normal temperature, adding polyvinylpyrrolidone and distilled water under stirring, cooling to normal temperature, stirring overnight, extracting the solution from the prepared solution by using an injector, fixing the injector filled with the silicon dioxide solution on a sample rack of electrostatic spinning equipment, connecting a positive electrode of a power supply with an injector needle, connecting a negative electrode of the power supply with a collector, starting a sample injection pump, turning on a high-voltage power supply to carry out electrostatic spinning, turning off the high-voltage power supply, the sample injection pump and the collector after the electrostatic spinning is finished, stopping spinning, and collecting a silicon dioxide crude product; calcining the crude silicon dioxide at high temperature, wherein the calcining temperature is 650 ℃, the temperature rise gradient is 1 ℃ per minute, the calcining time is 5 hours, and the cooling speed is 3 ℃ per minute;
2) dissolving the silicon dioxide calcined in the step 1 in an ethanol solution, and stirring for 30 minutes under ultrasonic;
3) reacting the silicon dioxide obtained in the step 2 with polyisocyanate to prepare modified silicon dioxide;
and mixing the modified silicon dioxide obtained by the preparation with dicumyl peroxide, methacrylate, ethyl acrylate and nano calcium carbonate, and extruding the mixture by a double-screw extruder to obtain the heat-insulating material.
2. The fuel gasification process system of claim 1, wherein a heating value meter is disposed on the outlet conduit.
3. The fuel gasification process system of claim 1, wherein the first feed tank, the second feed tank, and the raffinate recovery tank are each provided with a vent valve and a pressure gauge.
4. The fuel gasification process system of claim 1, wherein the heating medium in the heating device is a superconducting fluid.
5. The fuel gasification process system of claim 4, wherein the superconducting fluid is prepared from a raw material comprising, in mass percent: 0.5 to 4 percent of diglycolamine, 0.01 to 0.9 percent of sodium polyphosphate, 0.3 to 0.7 percent of benzotriazole derivative, 0.1 to 0.8 percent of sodium nitrite, 5 to 10 percent of sodium chloride and the balance of water.
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| CN201710797043.0A CN107686747B (en) | 2017-09-06 | 2017-09-06 | Fuel gasification process system capable of improving gas combustion rate |
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| CN201710797043.0A CN107686747B (en) | 2017-09-06 | 2017-09-06 | Fuel gasification process system capable of improving gas combustion rate |
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| CN2535679Y (en) * | 2001-05-08 | 2003-02-12 | 杨祥森 | Liquid-mmedium lifting auto-control mixed gas device made from ligt hydrocarbon oil |
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| 有机硅改性环氧树脂的合成;刘宝;《万方学术期刊数据库》;20120502;3,4 * |
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