CN112708470B - Device and method for producing synthesis gas by multi-nozzle gasification furnace - Google Patents
Device and method for producing synthesis gas by multi-nozzle gasification furnace Download PDFInfo
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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
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
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- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C10J2300/00—Details of gasification processes
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- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C10J2300/0959—Oxygen
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- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
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- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
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- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
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Abstract
The invention discloses a device and a method for producing synthesis gas by a multi-nozzle gasification furnace, the device sequentially comprises an atmospheric pulverized coal storage tank, a lock hopper and a feeding tank, a buffer tank and a screw conveyor are sequentially connected between a discharge pipe at the bottom of a material tank and a burner, the screw conveyor is sequentially connected with the burner and the gasification furnace, the gasification furnace is respectively connected with a washing tower and a slag breaker, the bottom of the slag breaker is connected with a slag lock hopper, the washing tower is sequentially connected with a high-pressure flash tank and a vacuum flash tank, the vacuum flash tank is connected with a tilting disk filter, and the tilting disk filter is connected with a settling tank. The invention can centralize the heat of the coal dust, quantitatively control the flow of the coal dust, improve the quantity of the conveyed coal dust, simultaneously have higher heat flux and combustion temperature and effectively reduce the water carrying quantity of the synthesis gas.
Description
Technical Field
The invention relates to the technical field of coal gasification, in particular to a device and a method for producing synthesis gas by a multi-nozzle gasification furnace.
Background
The petroleum and natural gas resources in China are insufficient, the characteristics of energy resources rich in coal, oil and gas are determined to greatly develop the coal chemical industry in China, and the coal gasification industry is the basic industry of the coal chemical industry, so the level of the coal gasification technology has important significance on the development of the coal chemical industry in China, the Texaco coal water slurry pressure gasification technology is introduced in the last eighties of China, the Shell dry coal powder pressure gasification technology is introduced in 2001, meanwhile, coal gasification technologies such as the fixed bed oxygen-enriched gasification technology, the dry coal powder pressure gasification technology, the multi-nozzle opposed dry coal powder pressure gasification technology and the like are respectively developed in China, and the coal gasification technologies developed in China at present are divided into three types, namely a lump coal gasification furnace, a gasification furnace and a coal gasification furnace according to fuel properties.
For example, in the 10 th coal slurry gasification technology development and its facing problems in 2004 of the journal of academia of china, coal engineering, a german process and its equipment are disclosed, which mainly include coal slurry preparation, a gasification furnace and a slag discharge system, and cooling and purification of high temperature coal gas. However, the process has the following disadvantages:
(1) the water content of the coal water slurry is high, the pulping concentration is about 59-61%, the cold coal gas efficiency is low, and the effective gas content is lower than that of an entrained flow gasifier;
(2) the requirement for coal is high;
(3) the service life of the burner of the gasification furnace is short, and is about 3500 h;
(4) the specific oxygen consumption is higher and is about 420 to 450m3/km3(CO+H2)；
(5) The ash melting point of the adopted coal is less than 1300 ℃, and the coal with high melting point cannot be adopted;
(6) the gasifier does not have a water-cooled wall, and refractory bricks are adopted to protect the gasifier, so that the maintenance cost is high.
For another example, a Shell coal gasification process is disclosed in "big nitrogen fertilizer" in journal of china engineering science and technology class, 2011 9 th "Shell coal gasification technology and its domestic application practice", but the Shell coal gasification technology has the following disadvantages:
(1) the SHELL gasification furnace is used for cooling high-temperature synthesis gas, and has strict requirements on equipment materials, complex waste boiler structure and high processing difficulty;
(2) the adopted coal type requires low ash fusion temperature and low ash content.
(3) The equipment investment cost is high.
For another example, chinese patent CN 101570699B discloses a gasification apparatus for solid fuel and a method for producing synthetic gas, the gasification process of an aerospace furnace belongs to a dry powder conveying entrained flow bed process, and ash-containing black water of the gasification furnace is conveyed to a settling tank for solid-liquid separation. The main process defects of the space furnace are as follows:
(1) the coal type adaptation range is wider than that of the Texaco gasification process, but the coal type adaptation range is not good for the coal types with high ash fusion points and high ash contents;
(2) the adopted pulverized coal locking bucket pressurizing and conveying system is relatively complex in control, pulverized coal conveying adopts pneumatic conveying, and the locking bucket frequently pressurizes to influence the operating pressure of the gasification furnace;
(3) the synthetic gas flows out from the lower liquid level of the chilling chamber, and the synthetic gas is easy to carry water;
also, chinese invention patent CN 98110616.1C discloses a multi-nozzle opposed coal water slurry or pulverized coal gasifier and its application, wherein the multi-nozzle opposed coal water slurry process is developed by the university of eastern science and industry and by the Yan Ore group, the main disadvantages of the multi-nozzle coal water slurry gasifier process are as follows:
(1) the four-nozzle gasification furnace is complicated to operate, one burner breaks down and can only be stopped, the service life of the burner is short, and the operation time of a single furnace is short;
(2) the installation of the refractory bricks of the gasification furnace is complicated, and the service life of the refractory bricks influences the operation cycle of the gasification furnace.
To sum up, a novel gasification furnace device which has reasonable structural design, can concentrate the heat of the pulverized coal, can quantitatively control the flow of the pulverized coal and improve the amount of the delivered pulverized coal, has higher heat flux and combustion temperature and avoids the water carrying of the synthesis gas is needed at present.
Disclosure of Invention
The invention aims to solve the technical problems that the existing gasification furnace for producing the synthesis gas has low density, low heat flux, low combustion temperature, water-carrying synthesis gas and the like in the coal powder entering the furnace.
In order to solve the technical problems, the technical scheme adopted by the invention is to provide a device for producing synthesis gas by a multi-nozzle gasification furnace, which comprises a normal-pressure coal powder storage tank, a lock hopper and a feeding tank which are connected through a pipeline group, wherein a buffer tank and a spiral conveyer are sequentially connected between a discharge pipe at the bottom of the feeding tank and a burner through the pipeline group, a certain differential pressure is preset between the feeding tank and the buffer tank, the spiral conveyer is sequentially connected with the burner and the gasification furnace, a burner is arranged on the burner, the gasification furnace is respectively connected with a water washing tower for receiving synthesis gas generated after coal powder is combusted and a slag breaking machine for receiving ash generated after coal powder is combusted through the pipeline group, the bottom of the slag breaking machine is connected with a slag lock hopper through the pipeline group, the water washing tower is sequentially connected with a high-pressure flash tank and a vacuum flash tank through the pipeline group, the vacuum flash tank is connected with a tilting pan filter for receiving the black water after flash evaporation through the pipeline set, and the tilting pan filter is connected with a settling tank for receiving the filtrate after fine slag filtration through the pipeline set.
In the scheme, the gasification furnace is sequentially divided into the combustion chamber and the chilling chamber from top to bottom, a chilling ring is arranged at the junction of the combustion chamber and the chilling chamber, and a water inlet for spraying chilling water is formed in the chilling ring.
In the scheme, the combustion chamber is internally provided with the annular cavity blowing air hole, and the flow direction of the annular cavity blowing air hole is parallel to the flame direction in the gasification furnace.
In the scheme, a water-cooled wall used for protecting a shell of the gasification furnace is arranged in a combustion chamber of the gasification furnace, the chilling ring is arranged below the water-cooled wall, and 4 infrared temperature measuring devices are arranged above the chilling ring.
In the scheme, the burner device is respectively provided with a burner cooling water inlet, a burner cooling water outlet, a water wall cooling water inlet and a water wall cooling water outlet, and the burner disc is internally provided with a cooling water pipeline.
In the scheme, the upper part of the gasification furnace is provided with a synthesis gas outlet, the synthesis gas outlet is connected with the water washing tower, and the synthesis gas outlet is arranged above the liquid level in the gasification furnace.
In the above scheme, the burner is provided with 2 cameras, the burner is composed of a coal pipe and an oxygen pipe, and the nozzle of the oxygen pipe is arranged at the tail end of the coal pipe.
In the scheme, the water washing tower is of a primary tower or a secondary tower group structure which is connected in series, and the water washing tower is internally provided with a spraying device.
In the above scheme, the combustor is a plurality of, and every the combustor matches respectively and is equipped with one screw conveyer, be connected with the flowmeter between feed tank and the buffer tank.
The invention also provides a method for producing synthesis gas by using the multi-nozzle gasification furnace, which comprises the following steps:
grinding pulverized coal into powder of 40-90 mu m by a coal mill, conveying the powder into a normal-pressure pulverized coal storage tank, conveying the pulverized coal in the normal-pressure pulverized coal storage tank under pressure by a lock hopper, and conveying the pulverized coal into a feeding tank;
maintaining a certain differential pressure between the feeding tank and the buffer tank, conveying pulverized coal from the bottom discharge pipe to the buffer tank through the feeding tank in a super-dense phase by virtue of the differential pressure, and controlling the pulverized coal feeding amount of the burner conveyed to the top of the gasification furnace by the buffer tank by adjusting the rotating speed of the bolt conveyor;
quantitative oxygen and ultra-dense phase coal powder are proportionally sprayed into a gasification furnace, the oxygen and carbon in the coal powder react at high temperature to generate synthesis gas, the pressure of the gasification furnace is increased to about 4.0MPa,the synthesis gas comprises CO and H as main components2Spraying cold water to the synthesis gas to cool the synthesis gas to 320-400 ℃, crushing the sprayed coarse slag by a slag breaker, then feeding the crushed coarse slag into a slag lock bucket, discharging the slag into a slag conveyor, and then discharging the slag from the slag conveyor in a waste slag form;
the sprayed synthesis gas is washed by two washing towers and enters the next process;
and (3) carrying out two-stage flash evaporation on black water generated after washing, then feeding the black water into the tilting pan type vacuum filter, after the tilting pan type vacuum filter filters fine ash, feeding filtrate into a settling tank, and discharging filter residues from a filter press system.
The invention has the following innovation points:
(1) the pulverized coal of the gasification furnace is conveyed by adopting an ultra-dense phase, so that the condition that the heat of flame is taken away by the conveying gas is avoided, the heat flux of coal flow combustion and the combustion temperature in the gasification furnace are improved, the temperature in the gasification furnace is 1800-2000 ℃, the gasification reaction time is reduced, compared with the gasification furnace of the same type, the single-furnace capacity is high, the temperature is high, and the CH in the synthesis gas is reduced4The content of (A);
(2) the gasifier adopts an integrated burner nozzle, so that the defect of overlarge volume caused by adopting a universal three-channel burner is avoided, the process pipeline complexity of the furnace end is reduced, meanwhile, the back mixing phenomenon of combustion media in the furnace is reduced by adopting a plurality of nozzles, and the temperature of the nozzle area is lower;
(3) the gasification furnace adopts two-stage washing of the synthetic gas, the synthetic gas does not flow out from the position below the liquid level of the slag water of the gasification furnace, and the defect of unstable pressure operation caused by liquid level fluctuation of the gasification furnace is avoided.
(4) The slag water treatment unit adopts the tilting pan filter to carry out solid-liquid separation before black water enters the settling tank, thereby greatly reducing the amount of solid phase particles entering the settling tank, reducing the frequency of tank settling accidents of the settling tank, and greatly reducing the labor cost of a filter press system for treating filter residues compared with the space furnace process.
Drawings
FIG. 1 is a flow chart of the operation of the apparatus of the present invention;
FIG. 2 is a schematic view of the structure of the gasification furnace of the present invention;
FIG. 3 is a schematic view of the structure of the burner of the present invention;
FIG. 4 is a schematic structural diagram of a first preferred embodiment of the present invention;
FIG. 5 is a schematic structural diagram of a first preferred embodiment of the present invention;
FIG. 6 is a schematic structural diagram of a first preferred embodiment of the present invention;
fig. 7 is a schematic structural diagram of a first preferred embodiment of the present invention.
Detailed Description
The invention is described in detail below with reference to the accompanying drawings.
The invention discloses a device and a method for producing synthesis gas by a multi-nozzle gasification furnace, and a person skilled in the art can appropriately improve process parameters by referring to the content. It is expressly intended that all such alterations and modifications which are obvious to those skilled in the art are deemed to be incorporated herein by reference, and that the techniques of the invention may be practiced and applied by those skilled in the art without departing from the spirit, scope and range of equivalents of the invention.
In the present invention, unless otherwise defined, scientific and technical terms used herein have the meanings that are commonly understood by those skilled in the art.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be considered limiting of the invention.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
It should be noted that the terms "first" and "second" in the description of the present invention are used merely for convenience in describing different components, and are not to be construed as indicating or implying a sequential relationship, relative importance, or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature.
As shown in fig. 1 to 7, the device for producing synthesis gas by using a multi-nozzle gasification furnace provided by the invention mainly comprises a coal conveying system, a burner 1, a gasification furnace 2, a water washing tower 9, a tilting pan filter 14 and the like, wherein the coal conveying system comprises a filter 5, a normal-pressure pulverized coal storage tank 3, a lock hopper 4 and a feed tank 8 which are sequentially connected through a pipeline group, and the coal conveying system is used for conveying in an ultra-dense phase and spraying pulverized coal into the gasification furnace 2 in an ultra-dense phase state. A buffer tank 16 and a screw conveyor 15 are sequentially connected between a bottom discharge pipe of the feeding tank 8 and the burner 1 through a pipeline group, a certain differential pressure is preset between the feeding tank 8 and the buffer tank 16, the screw conveyor 15 is sequentially connected with the burner 1 and the gasification furnace 2, the burner is installed on the burner 1 at the top of the gasification furnace 2, and the gasification furnace 2 is respectively connected with a synthetic gas (CO + H) generated after pulverized coal combustion through the pipeline group2) The water washing tower 9 and the slag breaking machine 6 for receiving ash generated after 6 pulverized coal combustion, the slag breaking machine 6 is connected to the bottom of the gasification furnace 2, the water washing tower 9 is of a one-stage tower or a two-stage tower group structure which is mutually connected in series, because the synthetic gas of the gasification furnace is not discharged from the lower part of the slag water liquid level like a space furnace, but directly enters the water washing tower after being sprayed by chilling water, in order to improve the slag removing effect, two-stage water washing is adopted, dust can be producedSynthesis gas with a content of less than 1%. The bottom of the slag breaker 6 is connected with a slag lock bucket 7 through a pipeline provided with a valve, a washing tower 9 is sequentially connected with a high-pressure flash tank 10 and a vacuum flash tank 11 for filtering black water of synthesis gas through a pipeline set, the vacuum flash tank 11 is connected with a tilting pan filter 14 for receiving the black water after flash evaporation through the pipeline set, the tilting pan filter 14 has the advantages of simple operation and low labor consumption compared with a filter press, and the tilting pan filter 14 is connected with a settling tank 12 for receiving filtrate after fine slag filtration through the pipeline set.
Preferably, the gasifier 2 is internally divided into a combustion chamber and a chilling chamber from top to bottom in sequence, a chilling ring is arranged at the junction of the combustion chamber and the chilling chamber, a water inlet 18 for spraying chilling water is arranged on the chilling ring, the chilling water of the water inlet 18 is sprayed to be vertical to the flow direction of the synthetic gas in the gasifier 2, and the chilling water is sprayed into the synthetic gas (CO + H) from the chilling ring2) In (1). An annular cavity blowing air hole 20 is arranged in the combustion chamber, and the flow direction of the annular cavity blowing air hole 20 is parallel to the flame direction in the gasification furnace 2. The coil type water-cooled wall 19 for protecting the shell of the gasification furnace is arranged in the combustion chamber of the gasification furnace 2, the coil type water-cooled wall 19 is used for separating the flame from the shell of the gasification furnace through a desalted water circulating pipe, the coil type water-cooled wall can produce saturated steam at high temperature to enter a steam pocket, and CO is introduced into the annular cavity space of the water-cooled wall and the shell during operation2The protective gas to prevent flame from channeling into the annular space, the coil pipe type water-cooled wall adopts the spiral installation of multitube, and the welding of the coil pipe of the water-cooled wall to the fire side has the anchor nail for hanging the sediment, the slag blanket can improve the life-span of the water-cooled wall.
The shell of the gasification furnace is provided with a chilling ring below the coil pipe type water-cooled wall 19, 2 infrared temperature measuring devices are arranged above the chilling ring, and CO is introduced into the infrared temperature measuring devices2Gas to protect the temperature measuring gun. The burner device is respectively provided with a combustion cooling water inlet 21, a combustion cooling water outlet 22, a water-cooled wall cooling water inlet 23 and a water-cooled wall cooling water outlet 24, and a cooling water pipeline is arranged in the burner disc. The gasification furnace 2 is provided with a synthetic gas outlet 17, the synthetic gas outlet 17 is connected with the water scrubber 9, two paths of synthetic gas are finally synthesized into one path of gas to enter the water scrubber, the synthetic gas outlet 17 is arranged above the liquid level in the gasification furnace 3, and the synthetic gas does not enter the liquid level of the slag chamber. Burner nozzleThe upper part of the burner is respectively provided with 2 cameras which are used for observing the combustion condition at the lower part of the burner in real time, the burner is respectively composed of a coal pipe 25 and an oxygen pipe 26, and the nozzle of the oxygen pipe 26 is arranged at the tail end of the coal pipe 25.
A plurality of burners are arranged on the burner plate 1, each burner is connected with a screw conveyer 15, and a flowmeter 13 is connected between the feeding tank 8 and the buffer tank 16. According to the diameter of the burner, the gasifier can adopt 3 nozzles, 4 nozzles and 6 nozzles, and compared with a single-burner gasifier, the multi-nozzle gasifier has the advantages of good reaction raw material mixing effect, large temperature field, short reaction time and small flame back-mixing phenomenon.
The invention provides a method for producing synthesis gas by a multi-nozzle gasification furnace, which adopts a process of 'entrained flow bed super dense phase coal dry powder gasification + water chilling', and comprises the following steps:
grinding pulverized coal into powder of 40-90 mu m by a coal mill, conveying the powder into a normal-pressure pulverized coal storage tank 3, conveying the pulverized coal in the normal-pressure pulverized coal storage tank 3 into a feeding tank 8 by pressurizing through a lock hopper 4;
maintaining a certain differential pressure between the feeding tank 8 and the buffer tank 16, conveying pulverized coal from a discharge pipe at the bottom to the buffer tank 16 in an ultra-dense phase by the feeding tank 8 through the differential pressure, and controlling the pulverized coal feeding amount conveyed to the top of the gasification furnace 2 by the buffer tank 16 through adjusting the rotating speed of the bolt conveyor 15;
quantitative oxygen and ultra-dense phase coal powder are proportionally sprayed into the gasification furnace 2, and the oxygen and carbon in the coal powder react at high temperature to generate synthesis gas (CO + H)2) Spraying cold water to the synthesis gas to cool the synthesis gas to 320-400 ℃, crushing the sprayed coarse slag by a slag breaker 6, then discharging the crushed coarse slag into a slag lock bucket 7, and discharging the crushed coarse slag in a slag salvaging machine in the form of waste slag;
the sprayed synthesis gas is washed by two washing towers to reduce the dust content of the synthesis gas, and then the synthesis gas enters the next working procedure;
and (3) carrying out two-stage flash evaporation on black water generated after washing, then feeding the black water into the tilting pan type vacuum filter, after the tilting pan type vacuum filter filters fine ash, feeding filtrate into a settling tank, and discharging filter residues from a filter press system.
Compared with the gasification process of the space furnace, the invention has the following advantages:
(1) the coal powder is conveyed into a buffer tank at the top of the gasification furnace in a super-dense phase way under the action of a magnetic spiral conveying device and differential pressure;
(2) 4 or more burners are arranged at the bottom of the buffer tank, the pulverized coal is conveyed into the burners by the magnetic spiral conveying device for combustion, conveying gas is not adopted, and the density of the pulverized coal can reach 700-800 kg/m3The heat of the pulverized coal is concentrated, and the temperature is higher than that of the Shell gasification furnace;
(3) in the process of purifying the synthesis gas, the synthesis gas flows into the water scrubber from the upper part of the liquid level of the slag slurry, the synthesis gas of the space furnace flows out from the lower part of the downcomer below the liquid level of the slag slurry, the problem of water carrying of the synthesis gas is easily caused by the fluctuation of the liquid level of the slag slurry, and the generated synthesis gas enters the next step after being subjected to the removal of fine ash in the 2-stage water scrubber;
(4) the ash-containing black water enters a tilting tray vacuum filter after two-stage flash evaporation, and clear liquid enters a settling tank.
The spiral conveyer is adopted to convey the ultra-dense-phase pulverized coal to enter the burner for combustion, the pulverized coal flow is controlled through the relation of rotating speed and flow, the bolt conveyer can adopt mechanical transmission or magnetic coupling transmission, the traditional mechanical seal is required to be adopted for the mechanical transmission, the mechanical seal is easy to damage and needs to be maintained and repaired at variable time, the leakage problem caused by the adoption of the mechanical seal can be avoided by adopting a magnetic coupling device, and the inner magnetic rotor in the coal line is driven to rotate through the rotation of the outer magnetic rotor, so that the pulverized coal is driven to flow. The outer rotor is a driving magnet, the inner rotor is a driven magnet, and the effect of quantitatively controlling the flow of the pulverized coal is achieved by controlling the rotating speed of the outer rotor.
The density of the coal powder in the coal conveying pipeline of the gasification furnace can reach 850kg/m3The density of the conveying coal powder of the space furnace is 350kg/m3Table 1 shows a comparison of the data for the space furnace and the gasification furnace of the present invention. In unit space, the quantity of coal powder injected in the state of ultra-dense phase is greatly higher than that of dense-phase conveying coal powder of space furnace, and the heat flux of ultra-dense phase coal flow in unit space for combustion is higher than that of dense-phase coal flow, so that the temp. in the gasification furnace is higher than that in the case of aeronautical furnaceThe temperature in the gasification furnace is the natural process.
TABLE 1 comparison of two coal fines transport process parameters
| Categories | Inner diameter of conveying pipe (mm) | Coal flow (h) | Transport speed (m/s) | Transport Density (kg/m)3) |
| This scheme | 50 | |
2～3 | 750～850 |
| HT-L | 50 | |
7～9 | 300～400 |
Under the condition of normal operation of a cooling water system, a washing system, a public and auxiliary system and the like, the invention verifies the relationship between the opening of partial valves and the gas flow in advance, and the gasification furnace mainly starts the process as follows:
(1) pulverized coal and pressurized conveying, wherein after the pulverized coal is ground by a medium-speed coal mill, hot air produced by a hot blast stove is conveyed to a bag type dust collector, and the bag type dust collector collects the pulverized coal and conveys the pulverized coal to a normal-pressure pulverized coal storage tank 3 through a spiral conveyor 15 at the lower part of the bag type dust collector; the lock hopper 4 feeds coal and produces coal through circulation of pressure relief, feeding, pressurization and discharging, and conveys coal powder to a feeding tank 8.
(2) Conveying and igniting pulverized coal, keeping the pressure of a feeding tank 8 at 2.0-1.5 MPa, keeping a buffer tank 16 at 1.5-1.2 MPa, keeping the pressure of a gasification furnace 2 at 1.0MPa, opening a return pipe from a coal conveying pipe to a normal-pressure pulverized coal storage tank 3 to start a screw conveyor 15, conveying the pulverized coal into the buffer tank 16, opening a pulverized coal cut-off valve at the bottom of the buffer tank 16 after a liquid level gauge of the buffer tank 16 displays that the material level reaches more than 80%, starting the magnetic screw conveyor 15, opening an oxygen valve after the flow of the pulverized coal is stable, and igniting by a natural gas ignition system.
(3) After ignition, the pressure of the feeding tank and the pressure of the buffer tank are increased, the feeding amount of the pulverized coal and the oxygen flow are synchronously increased until the pressure of the gasification furnace is increased to 4.0 +/-0.5 MPa, the pressure of the feeding tank is kept at 5.0-5.5 MPa, and the pressure of the buffer tank is kept at 4.5-4.2 MPa.
(4) According to the four pyrometer temperature curves on the upper side of the chilling section, the coal powder flow and the oxygen flow of each burner are adjusted by combining the camera observation effect on the top of the burner, so that the phenomenon of partial combustion in the furnace can be avoided.
(5) In the operation process of the gasification furnace, the slag breaking machine, the slag lock bucket pump and the black water pump are kept in an operation state, coarse slag enters the slag lock bucket through the slag breaking machine and is discharged to the slag dragging machine, fine slag is brought into the high-pressure flash evaporation separating tank and the vacuum flash evaporation separating tank by black water to separate steam, and then enters the tilting pan vacuum filter, and after the fine slag is removed, the fine slag enters the settling tank.
800t of dry pulverized coal (water content) is put into an 800t gasification furnace device<2%) can yield 220-240 × 106Nm3Synthesis gas of (CO + H)2) Specific process parameters can be seen in table 2.
The production data are as follows:
table 2800 t gasification furnace production data table
| Item | Unit of | Numerical value |
| Amount of dry coal powder | Ton/d | 800t |
| Syngas production | Nm3/d | 130×104 |
| Cold gas efficiency | ％ | 85 |
| Specific oxygen consumption | m3/km3(CO+H2) | 330 |
| Specific coal consumption | kg/km3(CO+H2) | 580 |
| Amount of coarse slag | Ton/d | 50 |
| Amount of fine slag | Ton/d | 480 |
| Chilling water | m3/d | 9000 |
The following are several preferred embodiments of the present invention
Example 1
As shown in figure 4, the technological conditions of 'single burner plus ultra-dense phase coal conveying' are adopted, the single burner is a traditional three-channel pulverized coal burner, the pulverized coal flow is adjusted by pressure difference, the gasification furnace is started, the synthetic gas generated in the combustion chamber is sprayed from the slag water level to the chilling water, the synthetic gas enters the water washing tower, most of the fine slag is removed, the synthetic gas enters the torch, the black water in the gasification furnace sequentially enters the high-pressure flash tank and the vacuum flash tank, and finally enters the settling tank, the coal slime is settled at the bottom of the tank by adding a flocculating agent in the settling tank, and the coal slime is pumped into a filter press by a pump to be subjected to solid-liquid separation.
The starting process is as follows:
(1) grinding and pressure conveying pulverized coal, wherein the ground pulverized coal is made of CO2After the gas is brought into the bag type dust collector, the gas enters a pulverized coal normal pressure pulverized coal storage tank, and the pulverized coal enters a feeding tank with the pressure close to that of the gasification furnace through the pressurized conveying of the lock hopper.
(2) Conveying and igniting the pulverized coal, keeping the pressure of a feeding tank at 2.0-1.8 MPa, keeping the pressure of a gasification furnace at 1.0MPa, opening a gas conveying valve on a pipeline of the feeding tank, bringing the pulverized coal into the gasification furnace by conveying gas, gradually closing the conveying gas, opening a valve on an oxygen pipeline after the flow of the pulverized coal is stable, and igniting by a natural gas ignition system.
Table 3 example 1 coal dust conveying process parameters
| Categories | Pressure difference (MPa) | Inner diameter of conveying pipe (mm) | Coal flow (t/h) | Transport speed (m/s) | Transport Density (kg/m)3) |
| Example 1 | 0.8 | 50 | 9～12 | 3.4～5.1 | 350～550 |
| Example 1 | 1.6 | 50 | 13～24 | 2.4～4.5 | 600～700 |
| Example 1 | 2 | 50 | 30～35 | 5.0～6.3 | 800～850 |
(3) After ignition, the pressure of a feeding tank is increased, the coal powder feeding amount and the oxygen flow are synchronously increased until the gasification furnace is pressurized to 4.0 +/-0.5 MPa, the black water flow and the chilling water flow are increased, and the temperature of the synthesis gas is maintained at 360-400 ℃.
The production data are shown in table 4 below,
TABLE 4 production data sheet of 1800t gasifier in example
| Item | Unit of | Numerical value |
| Amount of dry coal powder | Ton/d | 800t |
| Syngas production | Nm3/d | 105×104 |
| Cold gas efficiency | ％ | 70 |
| Specific oxygen consumption | m3/km3(CO+H2) | 350 |
| Specific coal consumption | kg/km3(CO+H2) | 590 |
| Amount of coarse slag | Ton/d | 50 |
| Amount of fine slag | Ton/d | 450 |
| Chilling water | m3/d | 7200 |
After drying, 20-30% of volatile components of the coal powder, 8% of ash and 55% of fixed carbon.
Example 2
As shown in figure 5, the coal powder conveying driven by differential pressure has the defect of unstable flow, the temperature control of the coal powder flow is achieved by adding a variable frequency magnetic spiral conveyor on the coal powder conveying pipeline,
adopt frequency conversion magnetic force screw conveyer, the advantage can guarantee the stability of buggy flow on the one hand, and on the other hand does not have the extravagant problem of buggy of differential pressure transport for before the ignition, there is not too much buggy in the gasifier, and table 5 is the buggy flow that adopts magnetic force screw conveyer.
Table 5 example 2 pulverized coal conveying process parameters
The starting process is as follows:
(1) grinding and pressure conveying pulverized coal, wherein the ground pulverized coal is brought into a bag type dust collector by CO2 gas, then enters a pulverized coal normal pressure pulverized coal storage tank, and the pulverized coal enters a feeding tank with the pressure close to that of a gasification furnace through pressure conveying of a lock hopper.
(2) Conveying and igniting the pulverized coal, keeping the pressure of a feeding tank at 1.5-2 MPa, keeping the pressure of a buffer tank at 1.2-1.5 MPa, opening a valve of the buffer tank which flows back to a normal-pressure pulverized coal storage tank, and maintaining the pulverized coal liquid level of the buffer tank at more than 80% by utilizing the differential pressure of the feeding tank and the buffer tank or a screw conveyor.
(3) And (3) keeping the pressure of the gasification furnace at 1.0MPa, opening a coal conveying stop valve at the upper part of the burner, adjusting the rotating speed of the magnetic screw conveyor, adjusting the flow of the pulverized coal to 8-10 t/h, and after the flow of the pulverized coal is stable, opening a valve on an oxygen pipeline and igniting by a natural gas ignition system.
(4) After ignition, the pressure of a feed tank and the pressure of a buffer tank are synchronously increased, the flow of pulverized coal and the flow of oxygen entering a burner are increased, the pressure of the gasification furnace is gradually increased to about 4.0MPa, and simultaneously, the flow of chilling water and black water is increased by an automatic temperature control program, so that the liquid levels of a slag chamber and a washing tower of the gasification furnace are maintained stable, and the outlet temperature of synthetic gas is stabilized.
The production data after installation of the magnetic screw conveyor are as follows:
TABLE 6 production data sheet of 2800 t gasifier in example
| Item | Unit of | Numerical value |
| Amount of dry coal powder | Ton/d | 800 |
| Syngas production | Nm3/d | 110～120×104 |
| Cold gas efficiency | ％ | 72～75 |
| Specific oxygen consumption | m3/km3(CO+H2) | 350 |
| Specific coal consumption | kg/km3(CO+H2) | 590 |
| Amount of coarse slag | Ton/d | 50 |
| Amount of fine slag | Ton/d | 450 |
| Chilling water | m3/d | 7200 |
After drying, 20-30% of volatile components of the coal powder, 8% of ash and 55% of fixed carbon
Example 3
As shown in fig. 6, in order to increase the heat flux of the gasification furnace and improve the capacity of the gasification furnace, the gasification furnace provided with the single burner has insufficient heat flux, the burners of the gasification furnace are modified, 3 burners are integrally installed on a burner tray, and simultaneously 1 washing tower is modified into 2 washing towers, so that the dust content of the synthesis gas is reduced.
3 burners and 1 ignition burner are installed on the burner plate, a spiral conveyer is installed on the coal conveying pipeline, the rotating speed parameters of the 3 spiral conveyers are merged into a driving program and a stopping SIS program, and a table 7 shows the relation between the rotating speed of the conveyer and the coal conveying flow.
Table 7 example 3 coal fines transport process parameters
The starting process is as follows:
(1) grinding and pressure conveying pulverized coal, wherein the ground pulverized coal is made of CO2After the gas is brought into the bag type dust collector, the gas enters a pulverized coal normal pressure pulverized coal storage tank, and the pulverized coal enters a feeding tank with the pressure close to that of the gasification furnace through the pressurized conveying of the lock hopper.
(2) Conveying and igniting the pulverized coal, keeping the pressure of a feeding tank within the range of 1.5-2 MPa, keeping the pressure of a buffer tank within the range of 1.2-1.5 MPa, opening a valve of the buffer tank which flows back to a normal-pressure pulverized coal storage tank, and maintaining the liquid level of the pulverized coal of the buffer tank at more than 80%.
(3) The pressure of the gasification furnace is kept at about 1.0MPa, a coal conveying stop valve at the upper part of each burner is opened, the rotating speed of a magnetic screw conveyor of each burner is adjusted, the total flow of pulverized coal of each burner is adjusted to 8-10 t/h, and after the flow of the pulverized coal is stable, a valve on an oxygen pipeline is opened, and ignition is carried out by a natural gas ignition system.
(4) After ignition, the pressure of a feeding tank and the pressure of a buffer tank are synchronously increased, the flow of pulverized coal and the flow of oxygen of each burner are synchronously increased according to a program, the pressure of the gasification furnace is increased to about 4.0MPa, the flow of chilling water and black water is increased by an automatic temperature control program, the liquid levels of a gasification furnace slag chamber and 2 washing towers are maintained to be stable, and the outlet temperature of the synthetic gas is stabilized.
The production data after installation of the magnetic screw conveyor are as follows:
TABLE 8 production data sheet of 3800 t gasifier in example
| Item | Unit of | Numerical value |
| Amount of dry coal powder | Ton/d | 850t |
| Syngas production | Nm3/d | 120×104 |
| Cold gas efficiency | ％ | 82 |
| Specific oxygen consumption | m3/km3(CO+H2) | 330 |
| Specific coal consumption | kg/km3(CO+H2) | 550 |
| Amount of coarse slag | Ton/d | 65 |
| Amount of fine slag | Ton/d | 450 |
| Chilling water | m3/d | 8500 |
After drying, 20-30% of volatile components of the coal powder, 8% of ash and 55% of fixed carbon
Example 4
In order to utilize the space of gasifier nozzle, further increase the heat flux of gasifier, improve the productivity of gasifier, increase a nozzle on the nozzle dish, totally 4 nozzles, the oblique nozzle dish of inserting of ignition nozzle.
Except that having increased 4 nozzles, increased the tilting pan filter in addition in black water filtration system, filtered black water before the subsider prerequisite, compare the technology with the subsider subsides the coal slime, the tilting pan filter has alleviateed the difficulty of subsider operation, has reduced the use of flocculating agent.
The 4 burners adopt coal nozzles with the diameter of 20mm, a magnetic spiral conveyor is installed on a coal powder pipeline of each burner, the rotating speed of the conveyor and the coal powder flow rate are approximately in a linear relation, and the stable control of the coal powder flow rate is achieved by controlling the rotating speed of the conveyor.
The starting process is as follows:
(1) grinding and pressure conveying pulverized coal, wherein the ground pulverized coal is made of CO2After the gas is brought into the bag type dust collector, the gas enters a pulverized coal normal pressure pulverized coal storage tank, and the pulverized coal enters a feeding tank with the pressure close to that of the gasification furnace through the pressurized conveying of the lock hopper.
(2) Conveying and igniting the pulverized coal, keeping the pressure of a feeding tank at 1.5-2 MPa, keeping the pressure of a buffer tank at 1.2-1.5 MPa, opening a valve of the buffer tank which flows back to a normal-pressure pulverized coal storage tank, and maintaining the pulverized coal liquid level of the buffer tank at more than 80% by utilizing the differential pressure of the feeding tank and the buffer tank or a screw conveyor.
(3) And (3) keeping the pressure of the gasification furnace at 1.0MPa, opening a coal conveying stop valve at the upper part of the burner, adjusting the rotating speed of each magnetic screw conveyor, adjusting the flow of pulverized coal of each burner to 8-10 t/h, opening a valve on an oxygen pipeline after the flow of the pulverized coal is stable, and igniting by a natural gas ignition system.
(4) After the flame is stabilized, the pressure of the feeding tank and the pressure of the buffer tank are synchronously increased, the rotating speed of the screw conveyor is adjusted, the flow of pulverized coal is increased, the flow of oxygen entering the gasifier is increased, the load of the gasifier is increased, the pressure of the gasifier is increased to about 4.0MPa, and the chilling water flow and the black water flow are automatically increased by an automatic control program according to the temperature of the synthesis gas.
The dust content can be reduced to below 1% by 2-stage water washing, most of coal slime can be filtered by the tilting disk filter, the labor consumption is lower than that of the filter press, and a table 9 is a production data table.
TABLE 9 production data sheet of 4800 t gasifier in example
| Item | Unit of | Numerical value |
| Amount of dry coal powder | Ton/d | 850～900 |
| Syngas production | Nm3/d | 130×104 |
| Cold gas efficiency | ％ | 80～85 |
| Specific oxygen consumption | m3/km3(CO+H2) | 320 |
| Specific coal consumption | kg/km3(CO+H2) | 530 |
| Amount of coarse slag | Ton/d | 45 |
| Amount of fine slag | Ton/d | 480 |
| Chilling water | m3/d | 9000 |
After drying, 20-30% of volatile components of the coal powder, 8% of ash and 55% of fixed carbon
The innovation points of the invention are as follows:
(1) the pulverized coal of the gasification furnace is conveyed by adopting an ultra-dense phase, so that the condition that the heat of flame is taken away by the conveying gas is avoided, the heat flux of coal flow combustion and the combustion temperature in the gasification furnace are improved, the temperature in the gasification furnace is 1800-2000 ℃, the gasification reaction time is reduced, compared with the gasification furnace of the same type, the single-furnace capacity is high, the temperature is high, and the CH in the synthesis gas is reduced4The content of (A);
(2) the gasifier adopts an integrated burner nozzle, so that the defect of overlarge volume caused by adopting a universal three-channel burner is avoided, the process pipeline complexity of the furnace end is reduced, meanwhile, the back mixing phenomenon of combustion media in the furnace is reduced by adopting a plurality of nozzles, and the temperature of the nozzle area is lower;
(3) the gasification furnace adopts two-stage washing of the synthetic gas, the synthetic gas does not flow out from the position below the liquid level of the slag water of the gasification furnace, and the defect of unstable pressure operation caused by liquid level fluctuation of the gasification furnace is avoided.
(4) The slag water treatment unit adopts the tilting pan filter to carry out solid-liquid separation before black water enters the settling tank, thereby greatly reducing the amount of solid phase particles entering the settling tank, reducing the frequency of tank settling accidents of the settling tank, and greatly reducing the labor cost of a filter press system for treating filter residues compared with the space furnace process.
The present invention is not limited to the above-mentioned preferred embodiments, and any structural changes made under the teaching of the present invention shall fall within the protection scope of the present invention, which has the same or similar technical solutions as the present invention.
Claims (9)
1. The method for producing the synthesis gas by the multi-nozzle gasification furnace is characterized by comprising the following steps:
the method for producing the synthesis gas by using the multi-nozzle gasification furnace uses a device for producing the synthesis gas by using the multi-nozzle gasification furnace, and the device for producing the synthesis gas by using the multi-nozzle gasification furnace comprises the following steps; comprises a normal pressure pulverized coal storage tank, a lock hopper and a feeding tank which are connected through a pipeline group, a buffer tank and a screw conveyer are sequentially connected between a discharge pipe at the bottom of the feeding tank and a burner through the pipeline group, a certain differential pressure is preset between the feeding tank and the buffer tank, the screw conveyer is sequentially connected with the burner and the gasification furnace, the burner is arranged on the burner, the gasification furnace is respectively connected with a water washing tower for receiving the synthesis gas generated after the combustion of the pulverized coal and a slag breaking machine for receiving the ash generated after the combustion of the pulverized coal through the pipeline groups, the bottom of the slag breaker is connected with a slag lock hopper through the pipeline set, the water washing tower is sequentially connected with a high-pressure flash tank and a vacuum flash tank through the pipeline set, the vacuum flash tank is connected with a tilting pan filter for receiving the black water after flash evaporation through the pipeline set, the tilting pan filter is connected with a settling tank for receiving filtrate after fine slag filtration through the pipeline group;
the method for producing the synthesis gas by the multi-nozzle gasification furnace comprises the following steps: grinding pulverized coal into powder of 40-90 mu m by a coal mill, conveying the powder into a normal-pressure pulverized coal storage tank, conveying the pulverized coal in the normal-pressure pulverized coal storage tank under pressure by a lock hopper, and conveying the pulverized coal into a feeding tank;
maintaining a certain differential pressure between the feeding tank and the buffer tank, conveying pulverized coal into the buffer tank from a discharge pipe at the bottom through the feeding tank in an ultra-dense phase by the differential pressure, controlling the pulverized coal feeding amount of a burner conveyed to the top of the gasification furnace by the buffer tank by adjusting the rotating speed of a screw conveyor, and carrying out thin film planting at 850kg/m in the coal conveying pipeline of the gasification furnace without carrying gas;
spraying quantitative oxygen and ultra-dense phase coal powder into a gasification furnace in proportion, reacting the oxygen and carbon in the coal powder at high temperature to generate synthesis gas, wherein the synthesis gas is CO and H2Spraying cold water to the synthesis gas to cool the synthesis gas to 320-400 ℃, crushing the sprayed coarse slag by a slag breaker, then feeding the crushed coarse slag into a slag lock bucket, discharging the slag into a slag conveyor, and then discharging the slag from the slag conveyor in a waste slag form;
the sprayed synthesis gas is washed by two washing towers and enters the next process;
and (3) carrying out two-stage flash evaporation on black water generated after washing, then feeding the black water into the tilting pan type vacuum filter, after the tilting pan type vacuum filter filters fine ash, feeding filtrate into a settling tank, and discharging filter residues from a filter press system.
2. The method for producing synthesis gas of a multi-nozzle gasifier according to claim 1, wherein the gasifier is divided into a combustion chamber and a chilling chamber in sequence from top to bottom, a chilling ring is arranged at the junction of the combustion chamber and the chilling chamber, and a water inlet for spraying chilling water is arranged on the chilling ring.
3. The method for producing synthesis gas of a multi-nozzle gasifier according to claim 2, wherein a ring cavity purge hole is provided in the combustion chamber, and the flow direction of the ring cavity purge hole is parallel to the flame direction in the gasifier.
4. The method for producing synthesis gas of a multi-nozzle gasifier according to claim 2, wherein a water-cooled wall for protecting a gasifier shell is provided in a combustion chamber of the gasifier, the quench ring is provided below the water-cooled wall, and 4 infrared temperature measuring devices are provided above the quench ring.
5. The method for producing synthesis gas of a multi-nozzle gasification furnace according to claim 4, wherein the burner is provided with a burner cooling water inlet, a burner cooling water outlet, a water wall cooling water inlet and a water wall cooling water outlet, and a cooling water pipeline is arranged in the burner.
6. The method for producing synthesis gas using a multi-nozzle gasifier as claimed in claim 1, wherein a synthesis gas outlet is opened at an upper portion of the gasifier, the synthesis gas outlet is connected to the water scrubber, and the synthesis gas outlet is disposed above a liquid level in the gasifier.
7. The method for producing syngas with multi-nozzle gasifier as claimed in claim 1, wherein 2 cameras are installed on the top of the burner for observing the flame inside the gasifier during the operation of the gasifier, the burners are respectively composed of a coal pipe and an oxygen pipe, and the nozzles of the oxygen pipe are installed at the ends of the coal pipe.
8. The method for producing synthesis gas of the multi-nozzle gasification furnace according to claim 1, wherein the water scrubber is a primary tower or a secondary tower set structure connected in series, and spray devices are arranged in the water scrubber.
9. The method for producing synthesis gas of the multi-nozzle gasification furnace according to claim 1, wherein the number of the burners is plural, each burner is provided with one screw conveyor in a matching manner, and a flow meter is connected between the feed tank and the buffer tank.
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