CN112852493A - Method and equipment for preparing synthesis gas by gasifying hard asphalt powder - Google Patents
Method and equipment for preparing synthesis gas by gasifying hard asphalt powder Download PDFInfo
- Publication number
- CN112852493A CN112852493A CN201911189090.2A CN201911189090A CN112852493A CN 112852493 A CN112852493 A CN 112852493A CN 201911189090 A CN201911189090 A CN 201911189090A CN 112852493 A CN112852493 A CN 112852493A
- Authority
- CN
- China
- Prior art keywords
- steam
- synthesis gas
- channel
- asphalt
- burner
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000010426 asphalt Substances 0.000 title claims abstract description 116
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 73
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 73
- 239000000843 powder Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 26
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 59
- 238000010438 heat treatment Methods 0.000 claims abstract description 38
- 239000007800 oxidant agent Substances 0.000 claims abstract description 22
- 239000000446 fuel Substances 0.000 claims abstract description 21
- 230000001590 oxidative effect Effects 0.000 claims abstract description 21
- 238000002844 melting Methods 0.000 claims abstract description 10
- 230000008018 melting Effects 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 71
- 230000008602 contraction Effects 0.000 claims description 31
- 239000002918 waste heat Substances 0.000 claims description 26
- 238000007599 discharging Methods 0.000 claims description 20
- 239000006227 byproduct Substances 0.000 claims description 18
- 238000002309 gasification Methods 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 15
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 238000005201 scrubbing Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 239000003570 air Substances 0.000 claims 3
- 238000004939 coking Methods 0.000 description 6
- 239000011295 pitch Substances 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000002679 ablation Methods 0.000 description 3
- 239000011339 hard pitch Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000000758 substrate Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000004806 packaging method and process Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 206010035148 Plague Diseases 0.000 description 1
- 241000607479 Yersinia pestis Species 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- 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
- C10J3/485—Entrained flow gasifiers
-
- 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
- C10J3/50—Fuel charging devices
- C10J3/506—Fuel charging devices for entrained flow gasifiers
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a method and equipment for preparing synthesis gas by gasifying hard asphalt powder. Wherein the apparatus comprises: a heating device and a converter; the heating equipment is used for melting the hard asphalt powder to obtain molten asphalt; the reformer is used for gasifying molten asphalt to obtain a first synthesis gas; the top of the reformer comprises a burner for feeding, and the burner is of a four-channel structure and comprises an oxidant channel, a first auxiliary gasifying agent channel, a fuel channel and a second auxiliary gasifying agent channel which are coaxially arranged from inside to outside; wherein the fuel channel is used for introducing molten asphalt. Wherein the method is carried out by the equipment, which comprises the following steps: melting the hard asphalt powder in the heating equipment to obtain molten asphalt; and conveying the molten asphalt into a converter to prepare a first synthesis gas.
Description
Technical Field
The invention relates to a method and equipment for producing synthesis gas from petroleum residues, in particular to a method and equipment for preparing synthesis gas by gasifying hard asphalt powder.
Background
The method converts cheap residual oil into products with high added value, and is a life line of the oil refining industry. Maximizing the utilization rate of the vacuum residue has become one of the goals pursued by enterprises. Solvent deasphalting is a method for processing heavy oil, the flow is simple, the energy consumption is low, the obtained deasphalted asphalt is good feed for catalytic cracking, but the outlet of the hard asphalt is always a problem. Market sales are limited due to the disadvantages of hard bitumen, such as high softening point, high sulfur and high nitrogen content. Therefore, there is a need to solve the problem of hard asphalt outtake. And (3) solidifying, slicing, granulating and packaging the hard asphalt to form a granular hard asphalt product, namely hard asphalt powder.
The hard asphalt has the advantages of high volatile matter content, high calorific value, less ash content, easy crushing and the like, and can be theoretically used for preparing synthesis gas by partial oxidation. However, from experimental conditions, the hard asphalt powder has small particle size and low bulk density, the hard asphalt powder slurry has high stirring difficulty and low slurry concentration, the concentration is only about 30 percent, and the gasification requirement of the coal water slurry is difficult to meet; further experiments show that the powder has general cohesiveness, the powder fluidity is between easy flowing and difficult flowing, and the requirement of pulverized coal gasification is difficult to meet. Therefore, gasification of hard asphalt powders must address the transportation of the feedstock.
The burner is one of key devices for preparing synthesis gas by converting various carbon-containing fuels. The burner not only effectively reduces the local backflow peroxide ablation at the end part of the flow channel, effectively solves the problem of short service life of the gasification burner, but also weakens the radiation of flame to the arch crown of the reformer and the end part of the burner, protects the refractory lining, reduces the temperature of the metal shell of the arch crown of the reformer and ensures the safe operation of the reformer. The existing deoiled asphalt gasification can adopt a three-channel burner, wherein a central channel is used for feeding oxygen, a second channel is used for feeding a mixture of steam and deoiled asphalt, and an outer channel is used for feeding oxygen; or a four-channel burner nozzle can be adopted, wherein the central channel is used for feeding oxygen, the second channel is used for feeding deoiled asphalt, the third channel is used for feeding oxygen, and the outer channel is used for feeding steam. However, the operation process of the existing deoiled asphalt burner is difficult to meet the requirement of gasifying the molten hard asphalt, because the temperature of the high-pressure superheated steam exceeds 400 ℃, if a three-channel burner is tried, the molten hard asphalt is mixed with the high-pressure steam, and the coking risk is large; if a four-channel burner is tried, oxygen in the central channel of the four-channel burner is directly contacted with molten hard asphalt in the second channel at the head of the burner, coking is easy to occur at the end part of the nozzle channel, and the burner is easy to ablate. Meanwhile, in the prior art, when the deoiled asphalt is converted, two oxidant channels are arranged in a three-channel burner or a four-channel burner, the requirement on the material of the burner needs to be improved, and the manufacturing cost of the burner is increased. In order to adapt to the high-efficiency gasification and long-period operation of the hard asphalt powder, the operation process of the burner is required to be improved.
Therefore, the transportation problem of the hard asphalt powder and the operation process of the burner in the reformer are two important technical problems that plague the hard asphalt powder as a gasification raw material.
Disclosure of Invention
The inventors of the present application, when attempting to convert hard pitch fines into syngas, found that problems of hard pitch fines being difficult to transport and of nozzles being prone to coking and ablation when referring to de-oiled pitch gasification nozzles. The invention innovatively provides a method and equipment for preparing synthesis gas by gasifying hard asphalt powder. The invention can convert hard asphalt powder into synthesis gas, and has the advantages of simple process flow and equipment structure, high energy utilization rate and low cost.
The invention discloses equipment for preparing synthesis gas by gasifying hard asphalt powder, which comprises the following components: a heating device and a converter;
the heating equipment is used for melting the hard asphalt powder to obtain molten asphalt; the reformer is used for gasifying molten asphalt to obtain a first synthesis gas;
the top of the reformer comprises a burner for feeding, and the burner is of a four-channel structure and comprises an oxidant channel, a first auxiliary gasifying agent channel, a fuel channel and a second auxiliary gasifying agent channel which are coaxially arranged from inside to outside; wherein the fuel channel is used for introducing molten asphalt.
In the invention, the hard asphalt powder is a granular hard asphalt product formed by solidifying, slicing, granulating and packaging hard asphalt (asphalt prepared by deep vacuum distillation or propane deasphalting process of crude oil, black solid and high softening point).
Preferably, the viscosity of the hard asphalt powder is 70-100cP at 200 ℃, 20-50cP at 250 ℃ and 5-20cP at 300 ℃.
In the present invention, the heating apparatus is the heating apparatus conventionally used in the art. Preferably, the heating equipment adopts a kettle type intermittent heat exchanger.
Preferably, the heating device comprises a first feeding hole, a second feeding hole, a first discharging hole and an asphalt conveying pipeline; the first feeding hole is a feeding channel of the hard asphalt powder; the second feed inlet is a feed channel of the first steam; the asphalt conveying pipeline is used for conveying the molten asphalt to the converter; and one end of the asphalt conveying pipeline is connected with the first discharge hole, and the other end of the asphalt conveying pipeline is connected with the fuel channel.
More preferably, the heating apparatus comprises a plurality of heating apparatuses connected in parallel to improve the ability of the apparatus to handle hard asphalt powders.
In the invention, the rest parts of the reformer except the burner part are of the structures which are conventional in the field. Preferably, the reformer employs a non-catalytic partial oxidation reactor.
In the invention, four channels in the burner adopt a gradually reducing structure.
Preferably, the inner contraction angle α of the oxidant channel is 50 to 90 degrees; and the inner contraction angle alpha refers to an included angle between the inner side wall of the oxidant passage and the end face of the outlet of the burner.
Preferably, the inner contraction angle beta of the first auxiliary gasification agent channel is 50-90 degrees; and the inner contraction angle beta refers to an included angle between the inner side wall of the first auxiliary gasifying agent channel and the end surface of the outlet of the burner.
Preferably, the internal contraction angle γ of the fuel passage is 50 to 90 degrees; and the internal contraction angle gamma refers to an included angle between the inner side wall of the fuel channel and the end face of the outlet of the burner.
Preferably, the inner contraction angle theta of the second auxiliary gasification agent channel is 50-90 degrees; and the inner contraction angle theta refers to an included angle between the inner side wall of the second auxiliary gasifying agent channel and the end face of the outlet of the burner.
Preferably, the internal contraction angle alpha is larger than or equal to the internal contraction angle beta is larger than or equal to the internal contraction angle gamma is larger than or equal to the internal contraction angle theta.
Preferably, a cooling system is further arranged on the periphery of the second auxiliary gasification agent channel.
More preferably, the cooling system may be a water circulation passage.
Preferably, the reformer further comprises a second discharge port and a first syngas delivery conduit; one end of the first synthesis gas conveying pipeline is connected with the second discharge hole and is used for conveying the first synthesis gas to post-treatment equipment and/or collecting equipment.
In a specific embodiment, in order to improve the energy utilization rate and reduce the cost, the equipment for preparing the synthesis gas by gasifying the hard asphalt powder further comprises a waste heat boiler and a washing device; the waste heat boiler is used for carrying out heat exchange with the first synthesis gas to obtain byproduct steam and second synthesis gas; and the washing equipment is used for post-treating the second synthesis gas and collecting to obtain a third synthesis gas.
Wherein the waste heat boiler is a waste heat boiler conventional in the field. Preferably, the waste heat boiler is a fire tube boiler.
Preferably, the waste heat boiler comprises a third feeding port, a fourth feeding port, a third discharging port, a fourth discharging port, a steam conveying pipeline and a second synthesis gas conveying pipeline; the third feeding port is connected with the first synthesis gas conveying pipeline and is used for feeding the first synthesis gas; the fourth feed port is used for conveying boiler feed water to the waste heat boiler; one end of the steam conveying pipeline is connected with the third discharge hole, and the other end of the steam conveying pipeline is simultaneously connected with the first feed hole, the first auxiliary gasifying agent channel and the second auxiliary gasifying agent channel; and the second synthesis gas conveying pipeline is connected with the fourth discharge hole and used for discharging the second synthesis gas out of the waste heat boiler.
Wherein, the washing equipment is the washing equipment conventional in the field.
Preferably, the scrubbing device comprises a fifth feed port and a fifth discharge port, and the fifth feed port is connected with the second synthesis gas conveying pipeline; and the fifth discharge hole is used for discharging the third synthetic gas out of the washing equipment.
In a specific embodiment, the equipment for preparing the synthesis gas by gasifying the hard asphalt powder further comprises a washing device, wherein the washing device is used for post-treating the first synthesis gas and collecting the second synthesis gas.
Wherein, the washing equipment is the washing equipment conventional in the field.
Preferably, the scrubbing device comprises a fifth feed port and a fifth discharge port, and the fifth feed port is connected with the first synthesis gas conveying pipeline; and the fifth discharge hole is used for discharging the second synthesis gas out of the washing equipment.
The invention discloses a method for preparing synthesis gas by gasifying hard asphalt powder, which is carried out by adopting the equipment for preparing synthesis gas by gasifying hard asphalt powder, and comprises the following steps:
melting the hard asphalt powder in the heating equipment to obtain molten asphalt;
and conveying the molten asphalt into the converter to prepare a first synthesis gas.
Preferably, the molten pitch is pumped into the reformer.
In a preferred embodiment, the amount of the hard asphalt powder entering the heating equipment is 0.5 to 20 t/h.
Preferably, the total amount of the hard asphalt powder entering the plurality of heating devices connected in parallel is 100-4000 t/d.
Preferably, the temperature of the molten asphalt is 250 to 300 ℃.
Preferably, the reformer is operated at 1200-1400 ℃ and at a pressure of 0.1-10Mpa, wherein the temperature and pressure of the first syngas is equal to the reformer operating temperature and pressure, as will be appreciated by those skilled in the art.
Preferably, the mass ratio of the oxidant in the oxidant channel to the hard asphalt powder entering the heating equipment is 0.8-1.0.
In the invention, the first steam can be introduced into the heating device for melting the hard asphalt powder.
Preferably, the mass ratio of the first steam to the hard asphalt powder entering the heating equipment is 0.3: 1-0.8: 1.
In one embodiment, the first syngas is introduced into a waste heat boiler, where heat exchange is performed to obtain byproduct steam and a second syngas.
The byproduct steam can be divided into four parts, namely first steam, second steam, third steam and fourth steam; the second steam is conveyed to the first auxiliary gasifying agent channel through a steam conveying pipeline to be used as a first auxiliary gasifying agent; the third steam is conveyed to a second auxiliary gasifying agent channel through a steam conveying pipeline to be used as a second auxiliary gasifying agent; and the fourth steam is byproduct steam, and the balance of the first steam, the second steam and the third steam is subtracted, and the fourth steam is sent to the air.
Wherein, the material of each passageway of nozzle is from inside to outside in proper order: the oxidant, the first auxiliary gasifying agent, the molten asphalt and the second auxiliary gasifying agent can realize the good atomization of the molten asphalt in the converter. The first auxiliary gasification agent channel is arranged between the oxidant channel and the fuel channel to isolate oxygen and molten pitch, so that the oxygen and the molten pitch are not directly mixed at the end of the burner, and the burning caused by coking and entrainment at the end of the burner is avoided. And a second auxiliary gasification agent channel is arranged to prevent the first synthesis gas in the converter from being sucked into a flame zone, so that the flame temperature is further reduced, and the refractory substrate of the converter is protected.
More preferably, the oxidant may be one or more of air, oxygen-enriched air.
More preferably, the first auxiliary gasifying agent may be the second steam.
More preferably, the second auxiliary gasifying agent may be the third steam.
Preferably, the mass ratio of the yield of the byproduct steam to the hard asphalt powder entering the heating equipment is 1.5: 1-2.5: 1.
Preferably, the total pressure of the byproduct steam is 8.0-12 MPa; and the total pressure of the byproduct steam is higher than the pressure of the first synthesis gas by more than 0.5 MPa.
Preferably, the mass ratio of the total amount of the second steam and the third steam entering the burner to the hard asphalt powder entering the heating equipment is 0.5: 1-1: 1.
Preferably, the second steam entering the first auxiliary gasifying agent channel accounts for 5-20% of the total amount of the second steam and the third steam entering the burner.
Preferably, the temperature of the second synthesis gas is preferably 250 ℃ to 400 ℃.
On the basis of the common knowledge in the field, the above preferred conditions can be combined randomly to obtain the preferred embodiments of the invention.
The reagents and starting materials used in the present invention are commercially available.
The positive progress effects of the invention are as follows:
(1) the problem of difficult transportation when hard pitch powder is used for preparing synthesis gas is solved.
(2) By improving the operation process of the burner, the burning caused by coking and entrainment at the end part of the burner is avoided, and the refractory substrate of the converter is protected.
(3) Conversion of hard asphalt powder to CO and H2The synthesis gas is mainly environment-friendly, the conversion rate of carbon element in the hard asphalt powder can reach 96.0-99.9%, and CO + H obtained by conversion2The content of the active carbon can reach 90-94%, the energy utilization efficiency is high, the process flow and the equipment structure are simple, and the investment is saved.
(4) According to the preferred embodiment of the invention, high-pressure steam is not required to be supplemented from the outside, and the problem of source of the high-pressure steam of a synthesis gas system for preparing asphalt powder is solved.
Drawings
Fig. 1 is a schematic structural diagram of the equipment for preparing synthesis gas by gasifying hard asphalt powder in example 1.
Wherein 100 is a heating device, 101 is a first feeding hole, 102 is a second feeding hole, 103 is a first discharging hole, 104 is an asphalt conveying pipeline, 200 is a reformer, 201 is a burner, 202 is a second discharging hole, 203 is a first synthesis gas conveying pipeline, 300 is a waste heat boiler, 301 is a third feeding hole, 302 is a fourth feeding hole, 303 is a third discharging hole, 304 is a fourth discharging hole, 305 is a steam conveying pipeline, 306 is a second synthesis gas conveying pipeline, 400 is a washing device, 401 is a fifth feeding hole, and 402 is a fifth discharging hole.
FIG. 2 is a schematic structural view of a burner of example 1.
Wherein 2011 is an oxidant channel, 2012 is a first auxiliary gasifying agent channel, 2013 is a fuel channel, 2014 is a second auxiliary gasifying agent channel, 2015 is a cooling system, alpha is an inner contraction angle alpha, beta is an inner contraction angle beta, and gamma is an inner contraction angle gamma.
Detailed Description
The invention is further illustrated by the following examples, which are not intended to limit the scope of the invention. The experimental methods without specifying specific conditions in the following examples were selected according to the conventional methods and conditions, or according to the commercial instructions.
In one embodiment of the present application, the parameters of the hard asphalt powder are as follows: the carbon residue content was 48.08 wt%, the sulfur content was 1.80 wt%, the nitrogen content was 1.83 wt%, the H/C was 1.18, the nickel content was 395. mu.g/g, the vanadium content was 302. mu.g/g, the calcium content was 861. mu.g/g, the saturates were 1.90 wt%, the aromatics were 9.07 wt%, the gum was 33.65 wt% asphaltene was 55.38 wt%, the softening point was 178 ℃, the particle size distribution was 2-500 μm, and the bulk density was 0.10g/cm3(ii) a The viscosity was 33cP at 250 deg.C, 26cP at 270 deg.C, and 20cP at 295 deg.C.
Example 1
The present embodiment provides an apparatus for preparing synthesis gas by gasifying hard asphalt powder, as shown in fig. 1-2, which comprises a heating apparatus 100, a converter 200, a waste heat boiler 300 and a washing apparatus 400.
Wherein, the heating device 100 is used for melting the hard asphalt powder to obtain molten asphalt; the reformer 200 is configured to gasify molten asphalt to obtain a first syngas; the top of the reformer 200 comprises a burner 201 for feeding, and the burner 201 is of a four-channel structure and comprises an oxidant channel 2011, a first auxiliary gasifying agent channel 2012, a fuel channel 2013 and a second auxiliary gasifying agent channel 2014 which are coaxially arranged from inside to outside; wherein, the fuel channel 2013 is used for introducing molten asphalt. A cooling system 2015 is also provided around the periphery of the second auxiliary gasification-agent channel 2014.
Wherein, the heating device 100 adopts a kettle type intermittent heat exchanger. Wherein, the heating device 100 comprises a first feeding hole 101, a second feeding hole 102, a first discharging hole 103 and an asphalt conveying pipeline 104; the first feed port 101 is a feed passage for hard asphalt powder; the second feed port 102 is a feed passage for the first steam; the asphalt delivery pipe 104 is used for delivering molten asphalt to the reformer 200; one end of the asphalt delivery pipe 104 is connected with the first discharge port 103, and the other end is connected with the fuel passage 2013.
Wherein, the reformer 200 employs a non-catalytic partial oxidation reactor. Wherein, the reformer 200 further comprises a second discharge port 202 and a first syngas conveying pipe 203; one end of the first syngas conveying pipe 203 is connected to the second outlet 202, and can be used for conveying the first syngas to the next equipment, in this embodiment, the waste heat boiler 300.
Wherein, the material of each passageway of nozzle 201 is from inside to outside in proper order: the oxidant, the first auxiliary gasifying agent, the fuel and the second auxiliary gasifying agent can realize the good atomization of the molten asphalt in the reformer 200. By arranging the first auxiliary gasifying agent channel 2012 between the oxidant channel 2011 and the fuel channel 2013 to isolate oxygen and molten pitch, the oxygen and the molten pitch are not directly mixed at the end of the burner 201, and ablation caused by coking and entrainment at the end of the burner 201 is avoided. And a second auxiliary gasifying agent channel 2014 is arranged to prevent the entrainment of the first synthesis gas in the converter from entering a flame zone, so that the flame temperature is further reduced, and the refractory substrate of the converter 200 is protected.
Wherein the oxidant is oxygen. Wherein, the first auxiliary gasifying agent is second steam. Wherein, the second auxiliary gasifying agent is third steam. Wherein the cooling system 2015 is a water circulation channel.
Wherein, four channels in the burner 201 adopt a tapered structure.
The inner contraction angle α of the oxidant passage 2011 is 70 degrees, the inner contraction angle β of the first auxiliary gasifying agent passage 2012 is 70 degrees, the inner contraction angle γ of the fuel passage 2013 is 70 degrees, and the inner contraction angle θ of the second auxiliary gasifying agent passage 2014 is 70 degrees.
The waste heat boiler 300 is configured to exchange heat with the first syngas to obtain byproduct steam and a second syngas. Among them, the waste heat boiler 300 employs a fire tube boiler. Wherein, the waste heat boiler 300 comprises a third feeding port 301, a fourth feeding port 302, a third discharging port 303, a fourth discharging port 304, a steam conveying pipeline 305 and a second synthesis gas conveying pipeline 306; the third feeding port 301 is connected with the first synthesis gas conveying pipeline 203 and is used for feeding the first synthesis gas; the fourth feed inlet 302 is for feeding boiler feed water to the waste heat boiler 300; one end of the steam conveying pipeline 305 is connected with the third discharge hole 303, and the other end of the steam conveying pipeline is simultaneously connected with the first feed hole 101, the first auxiliary gasifying agent channel 2012 and the second auxiliary gasifying agent channel 2014; a second syngas delivery conduit 306 is connected to the fourth outlet 304 for discharging the second syngas out of the waste heat boiler 300.
Wherein the scrubbing apparatus 400 is used to post-treat the second syngas and collect a third syngas. Wherein the scrubbing apparatus 400 comprises a fifth inlet 401 and a fifth outlet 402, the fifth inlet 401 is connected to the second syngas conveying pipe 306; the fifth discharge port 402 is used to discharge the third syngas out of the scrubbing apparatus 400.
In this embodiment, a method for preparing synthesis gas by gasifying hard asphalt powder is adopted, and the method is performed by using the above apparatus for preparing synthesis gas by gasifying hard asphalt powder, and includes the following steps:
introducing the first steam into the heating equipment 100, and melting the hard asphalt powder in the heating equipment 100 to obtain molten asphalt; conveying the molten asphalt into a reformer 200 in a pumping manner to prepare a first synthesis gas; introducing the first synthesis gas into a waste heat boiler 300, and performing heat exchange in the waste heat boiler 300 to obtain byproduct steam and second synthesis gas; the second syngas is passed to the scrubbing apparatus 400.
The byproduct steam can be divided into four parts, namely first steam, second steam, third steam and fourth steam; the second steam is conveyed to the first auxiliary gasifying agent channel 2012 through the steam conveying pipe 305 as a first auxiliary gasifying agent; the third steam is conveyed to the second auxiliary gasifying agent passage 2014 through the steam conveying pipeline 305 to be used as a second auxiliary gasifying agent; and the fourth steam is the byproduct steam, and the balance of the first steam, the second steam and the third steam is deducted, and is sent out to the air.
In this example, the physical and chemical parameters of the hard asphalt powder are shown in table 1, and the main process parameters are shown in table 2.
TABLE 1 physical and chemical parameters of asphalt powder
TABLE 2 Main Process parameters
Claims (10)
1. An apparatus for preparing synthesis gas by gasifying hard asphalt powder, which is characterized by comprising: a heating device and a converter;
the heating equipment is used for melting the hard asphalt powder to obtain molten asphalt; the reformer is used for gasifying molten asphalt to obtain a first synthesis gas;
the top of the reformer comprises a burner for feeding, and the burner is of a four-channel structure and comprises an oxidant channel, a first auxiliary gasifying agent channel, a fuel channel and a second auxiliary gasifying agent channel which are coaxially arranged from inside to outside; wherein the fuel channel is used for introducing molten asphalt.
2. The apparatus of claim 1, wherein said heating apparatus comprises a first inlet, a second inlet, a first outlet, and an asphalt delivery conduit; the first feeding hole is a feeding channel of the hard asphalt powder; the second feed inlet is a feed channel of the first steam; the asphalt conveying pipeline is used for conveying the molten asphalt to the converter; and one end of the asphalt conveying pipeline is connected with the first discharge hole, and the other end of the asphalt conveying pipeline is connected with the fuel channel.
3. The apparatus of claim 1, wherein the four-channel structure in the burner is a tapered structure;
preferably, the inner contraction angle α of the oxidant channel is 50 to 90 degrees; the inner contraction angle alpha refers to an included angle between the inner side wall of the oxidant passage and the end face of the outlet of the burner;
preferably, the inner contraction angle beta of the first auxiliary gasification agent channel is 50-90 degrees; the inner contraction angle beta refers to an included angle between the inner side wall of the first auxiliary gasifying agent channel and the end face of the outlet of the burner;
preferably, the internal contraction angle γ of the fuel passage is 50 to 90 degrees; the inner contraction angle gamma refers to an included angle between the inner side wall of the fuel channel and the end face of the outlet of the burner;
preferably, the inner contraction angle theta of the second auxiliary gasification agent channel is 50-90 degrees; the inner contraction angle theta refers to an included angle between the inner side wall of the second auxiliary gasifying agent channel and the end face of the outlet of the burner;
preferably, the internal contraction angle alpha is more than or equal to the internal contraction angle beta is more than or equal to the internal contraction angle gamma is more than or equal to the internal contraction angle theta;
preferably, a cooling system is further arranged at the periphery of the second auxiliary gasification agent channel;
more preferably, the cooling system is a water circulation channel;
preferably, the heating equipment adopts a kettle type intermittent heat exchanger;
preferably, the reformer employs a non-catalytic partial oxidation reactor.
4. The apparatus of claim 2, wherein said reformer further comprises a second outlet and a first syngas delivery conduit; one end of the first synthesis gas conveying pipeline is connected with the second discharge hole and is used for conveying the first synthesis gas to post-treatment equipment and/or collecting equipment;
preferably, the heating device comprises a plurality of heating devices connected in parallel.
5. The apparatus of claim 4, further comprising a waste heat boiler and a scrubbing apparatus; the waste heat boiler is used for carrying out heat exchange with the first synthesis gas to obtain byproduct steam and second synthesis gas; the washing equipment is used for post-treating the second synthesis gas and collecting to obtain a third synthesis gas;
preferably, the waste heat boiler comprises a third feeding port, a fourth feeding port, a third discharging port, a fourth discharging port, a steam conveying pipeline and a second synthesis gas conveying pipeline; the third feeding port is connected with the first synthesis gas conveying pipeline and is used for feeding the first synthesis gas; the fourth feed port is used for conveying boiler feed water to the waste heat boiler; one end of the steam conveying pipeline is connected with the third discharge hole, and the other end of the steam conveying pipeline is simultaneously connected with the first feed hole, the first auxiliary gasifying agent channel and the second auxiliary gasifying agent channel; the second synthesis gas conveying pipeline is connected with the fourth discharge hole and used for discharging the second synthesis gas out of the waste heat boiler;
preferably, the waste heat boiler adopts a fire tube boiler;
preferably, the scrubbing device comprises a fifth feed port and a fifth discharge port, and the fifth feed port is connected with the second synthesis gas conveying pipeline; and the fifth discharge hole is used for discharging the third synthetic gas out of the washing equipment.
6. The apparatus of claim 2, further comprising a scrubbing device for post-treating the first syngas to collect a second syngas;
preferably, the scrubbing device comprises a fifth feed port and a fifth discharge port, and the fifth feed port is connected with the first synthesis gas conveying pipeline; and the fifth discharge hole is used for discharging the second synthesis gas out of the washing equipment.
7. A method for preparing synthesis gas by gasifying hard asphalt powder, the method being carried out by using the equipment according to any one of claims 1 to 6, and being characterized by comprising the following steps:
melting the hard asphalt powder in the heating equipment to obtain molten asphalt;
and conveying the molten asphalt into the converter to prepare a first synthesis gas.
8. The method of claim 7, wherein said molten pitch is pumped into said reformer;
preferably, the viscosity of the hard asphalt powder is 70-100cP at 200 ℃, 20-50cP at 250 ℃ and 5-20cP at 300 ℃;
preferably, the temperature of the molten asphalt is 250-300 ℃;
preferably, the operation temperature of the conversion furnace is 1200-1400 ℃, and the pressure is 0.1-10 MPa.
9. The method of claim 7, wherein the mass ratio of the oxidizing agent to the hard asphalt powder entering the heating device is 0.8 to 1.0;
preferably, first steam is passed into the heating device for melting the hard asphalt powder; the mass ratio of the first steam to the hard asphalt powder entering the heating equipment is 0.3: 1-0.8: 1.
10. The method of claim 9, wherein the first syngas is passed to the waste heat boiler where heat is exchanged to produce a byproduct stream and a second syngas;
preferably, the byproduct steam is divided into four parts, namely the first steam, the second steam, the third steam and the fourth steam; the second steam is conveyed to the first auxiliary gasifying agent channel through the steam conveying pipeline to serve as the first auxiliary gasifying agent; the third steam is conveyed to the second auxiliary gasifying agent channel through the steam conveying pipeline to be used as the second auxiliary gasifying agent; the fourth steam is the byproduct steam minus the balance of the first steam, the second steam and the third steam and is sent out to the air;
preferably, the materials of each channel of the burner are as follows from inside to outside in sequence: an oxidant, a first auxiliary gasifying agent, the molten state asphalt and a second auxiliary gasifying agent;
more preferably, the oxidant is one or more of air, oxygen and oxygen-enriched air;
more preferably, the first auxiliary gasification agent is the second steam;
more preferably, the second auxiliary gasification agent is the third steam;
preferably, the mass ratio of the yield of the byproduct steam to the hard asphalt powder entering the heating equipment is 1.5: 1-2.5: 1;
preferably, the total pressure of the byproduct steam is 8.0-12 MPa; the total pressure of the byproduct steam is higher than the pressure of the first synthesis gas by more than 0.5 MPa;
preferably, the mass ratio of the total amount of the second steam and the third steam entering the burner to the hard asphalt powder entering the heating equipment is 0.5: 1-1: 1;
preferably, the second steam entering the first auxiliary gasifying agent channel accounts for 5-20% of the total amount of the second steam and the third steam entering the burner;
preferably, the temperature of the second synthesis gas is 250 ℃ to 400 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911189090.2A CN112852493A (en) | 2019-11-28 | 2019-11-28 | Method and equipment for preparing synthesis gas by gasifying hard asphalt powder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911189090.2A CN112852493A (en) | 2019-11-28 | 2019-11-28 | Method and equipment for preparing synthesis gas by gasifying hard asphalt powder |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112852493A true CN112852493A (en) | 2021-05-28 |
Family
ID=75985234
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911189090.2A Pending CN112852493A (en) | 2019-11-28 | 2019-11-28 | Method and equipment for preparing synthesis gas by gasifying hard asphalt powder |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112852493A (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101498441A (en) * | 2009-02-12 | 2009-08-05 | 中国船舶重工集团公司第七一一研究所 | Gasification furnace burner used for asphalt gasification |
| CN102492477A (en) * | 2011-11-11 | 2012-06-13 | 上海交通大学 | Hierarchical oxygen supply and controllable flame coal water slurry entrained bed combined nozzle |
| CN202392795U (en) * | 2011-12-06 | 2012-08-22 | 中国石油化工股份有限公司 | Gasification furnace burner used for asphalt gasification |
| CN102876345A (en) * | 2012-10-30 | 2013-01-16 | 中国石油化工股份有限公司 | Hard asphalt granulation method and device thereof |
| JP2013024451A (en) * | 2011-07-19 | 2013-02-04 | Electric Power Dev Co Ltd | Gasification burner |
| CN204058390U (en) * | 2014-03-28 | 2014-12-31 | 上海锅炉厂有限公司 | Solid fuel classification gasification-burning double bed polygenerations systeme |
| CN105271115A (en) * | 2015-11-25 | 2016-01-27 | 华东理工大学 | Gaseous hydrocarbon reformer nozzle |
| CN105731376A (en) * | 2016-01-12 | 2016-07-06 | 华东理工大学 | Partial oxidation process burner and application thereof |
| CN207294700U (en) * | 2017-09-14 | 2018-05-01 | 中国华能集团清洁能源技术研究院有限公司 | A kind of four-way process burner structure for double-section dry coal powder pressure gasifying technology |
| CN109777462A (en) * | 2017-11-10 | 2019-05-21 | 神华集团有限责任公司 | High softening point bitumen and its continuous producing method and system |
| CN211497524U (en) * | 2019-11-28 | 2020-09-15 | 华东理工大学 | Equipment for preparing synthesis gas by gasifying hard asphalt powder |
-
2019
- 2019-11-28 CN CN201911189090.2A patent/CN112852493A/en active Pending
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101498441A (en) * | 2009-02-12 | 2009-08-05 | 中国船舶重工集团公司第七一一研究所 | Gasification furnace burner used for asphalt gasification |
| JP2013024451A (en) * | 2011-07-19 | 2013-02-04 | Electric Power Dev Co Ltd | Gasification burner |
| CN102492477A (en) * | 2011-11-11 | 2012-06-13 | 上海交通大学 | Hierarchical oxygen supply and controllable flame coal water slurry entrained bed combined nozzle |
| CN202392795U (en) * | 2011-12-06 | 2012-08-22 | 中国石油化工股份有限公司 | Gasification furnace burner used for asphalt gasification |
| CN102876345A (en) * | 2012-10-30 | 2013-01-16 | 中国石油化工股份有限公司 | Hard asphalt granulation method and device thereof |
| CN204058390U (en) * | 2014-03-28 | 2014-12-31 | 上海锅炉厂有限公司 | Solid fuel classification gasification-burning double bed polygenerations systeme |
| CN105271115A (en) * | 2015-11-25 | 2016-01-27 | 华东理工大学 | Gaseous hydrocarbon reformer nozzle |
| CN105731376A (en) * | 2016-01-12 | 2016-07-06 | 华东理工大学 | Partial oxidation process burner and application thereof |
| CN207294700U (en) * | 2017-09-14 | 2018-05-01 | 中国华能集团清洁能源技术研究院有限公司 | A kind of four-way process burner structure for double-section dry coal powder pressure gasifying technology |
| CN109777462A (en) * | 2017-11-10 | 2019-05-21 | 神华集团有限责任公司 | High softening point bitumen and its continuous producing method and system |
| CN211497524U (en) * | 2019-11-28 | 2020-09-15 | 华东理工大学 | Equipment for preparing synthesis gas by gasifying hard asphalt powder |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8685120B2 (en) | Method and apparatus to produce synthetic gas | |
| CN101412929B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| KR101633951B1 (en) | Process and apparatus for utilizing the enthalpy of a synthesis gas by means of additional and post-gassing of renewable fuels | |
| US8814961B2 (en) | Various methods and apparatuses for a radiant-heat driven chemical reactor | |
| CN104342212B (en) | PC-FB hydropyrolysis and gasification coupling method | |
| CN101418239A (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| AU2012350785A1 (en) | Method and device for the entrained flow gasification of solid fuels under pressure | |
| CN104611063B (en) | A kind of airflow bed gasification furnace | |
| US8741179B2 (en) | Process and equipment for reforming gasification gas | |
| CN101418240A (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN102268300B (en) | Coal liquefaction residue and coal water slurry combined gasification nozzle and application thereof | |
| CN100374531C (en) | Method for preparing synthetic gas by three-channel nozzle and partial oxidation of solid carbon-containing substance | |
| CN211497524U (en) | Equipment for preparing synthesis gas by gasifying hard asphalt powder | |
| CN101418238B (en) | High temperature gasification technological process and system for preparing synthesis gas by using biomass | |
| CN102939361B (en) | Thermal decomposition coal gasification method and thermal decomposition coal gasification device | |
| CN100535517C (en) | Multi-channel liquid stage fuel partial oxidation generating synthesis gas burner and uses thereof | |
| CN109054901A (en) | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device | |
| CN112852493A (en) | Method and equipment for preparing synthesis gas by gasifying hard asphalt powder | |
| CN112680249B (en) | Organic solid waste pressure gasification system and method | |
| CN113150832A (en) | Self-heating three-section type biomass low-tar carbon gas co-production regulation and control device | |
| CN113025382A (en) | Radiation waste pot, gasification furnace comprising same and gasification method | |
| CN108774547A (en) | The system and method for coal liquefaction residue producing synthesis gas | |
| US20150014594A1 (en) | Process and apparatus for molten slag gasification of solid fuels | |
| CN205710606U (en) | Steam jet ejector and the system including steam jet ejector | |
| JP6018289B2 (en) | Integrated process for gasification and power generation of whole crude oil in membrane wall gasifier |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |