阅读说明：本技术 一种高含湿有机物料产生合成气的气化装置 (Gasification device for producing synthesis gas from high-moisture organic material ) 是由 陈德珍 梅振飞 冯昱恒 于 2019-09-26 设计创作，主要内容包括：本发明提供了一种高含湿有机物料产生合成气的气化装置,属于气化装置领域。本发明提供的高含湿有机物料产生合成气的气化装置,包括：进料装置、1-3个热解反应器、气化反应器、固体颗粒分离器、残焦箱、气体净化装置以及燃烧装置。其中,所述热解反应器竖直设置,所述气化反应器水平设置,二者呈L型设置。本发明避免了催化剂的老化、失效引起的系统运行不稳定的问题,同时充分利用了水蒸汽的潜热、挥发份和热解炭的显热与化学热,节约了能耗、提高了经济性,还可以在必要的情况下非常方便地加入便宜的白云石等活化剂于高含湿的物料中作为催化剂而不需要专门设置放置催化剂的昂贵反应器。(The invention provides a gasification device for generating synthesis gas from high-moisture organic materials, and belongs to the field of gasification devices. The invention provides a gasification device for producing synthesis gas by using high moisture-containing organic materials, which comprises: the device comprises a feeding device, 1-3 pyrolysis reactors, a gasification reactor, a solid particle separator, a residual coke box, a gas purification device and a combustion device. Wherein, pyrolysis reactor vertical setting, gasification reactor horizontal setting, the two is the L type setting. The invention avoids the problem of unstable system operation caused by aging and failure of the catalyst, simultaneously fully utilizes the latent heat and volatile matters of water vapor and the sensible heat and chemical heat of pyrolytic carbon, saves energy consumption, improves the economical efficiency, and can conveniently add cheap activating agents such as dolomite and the like into high-moisture materials as the catalyst under the necessary condition without specially arranging an expensive reactor for placing the catalyst.)

1. A gasification apparatus for producing synthesis gas from a high moisture content organic material, comprising:

the feeding device is used for adding the high-moisture organic material;

one end of each pyrolysis reactor is connected with the feeding device, and the pyrolysis reactors are used for drying and pyrolyzing the high-moisture organic materials;

the gasification reactor is connected with one end of the pyrolysis reactor, which is far away from the feeding device, and is used for carrying out gasification reaction on pyrolysis reaction products;

the solid particle separator is connected with the gasification reactor and is used for separating solid particles and gas generated by the gasification reaction;

a residual coke box connected with the gasification reactor and the solid particle separator and used for receiving residual coke generated in the gasification reactor and the solid particle separator;

a gas purification device connected to the solid particle separator for receiving and purifying the gas generated in the gasification reactor; and

the combustion device is used for generating high-temperature flue gas by combusting gas,

wherein, pyrolysis reactor vertical setting, gasification reactor horizontal setting, the two is the L type setting.

2. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the high moisture content organic material is an organic material with a water content of not more than 55 wt%.

3. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the high moisture content organic material contains dolomite and/or nickel nitrate activator.

4. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

and the upper part of the pyrolysis reactor is provided with a disturbance device for pushing and disturbing the materials in the pyrolysis reactor.

5. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the working temperature of the pyrolysis reactor is 450-650 ℃.

6. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the working temperature of the gasification reactor is 800-900 ℃.

7. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the gas purification device is selected from any one of a Venturi type alkali scrubber with a defoaming measure, a spray type alkali scrubber with a defoaming measure and a sieve plate tower type alkali scrubber with a defoaming measure, and is combined with the active coke adsorption tower.

8. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the gasification reactor is selected from a screw propulsion reactor or a rotary kiln reactor.

9. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein the combustion apparatus comprises:

a burner directly or indirectly communicating with the gas purification apparatus, the burner using gas discharged from the gas purification apparatus as fuel; and

and the combustion chamber is used for combusting gas and generating high-temperature flue gas, and the high-temperature flue gas is introduced into the outer layer and the inner side of the gasification reactor and the outer side of the pyrolysis reactor.

10. A gasification plant for the production of synthesis gas from high moisture organic matter as claimed in claim 1 wherein:

wherein, the solid particle separator is selected from any one of a cyclone dust collector, a foam metal filter and a ceramic filter.

Technical Field

The invention relates to a gasification device, in particular to a gasification device for generating synthesis gas from high-moisture organic materials, and belongs to the field of gasification devices.

Background

Due to low economic benefit and strict environmental protection regulations, the current methods for disposing garbage, sludge and agricultural wastes (such as straws, rice husks and the like) are generally such as landfill, composting and incineration, but the traditional methods do not realize the conversion of waste clean energy.

Currently, pyrolysis and gasification are considered waste clean energy technologies. These techniques can reduce the flue gas volume and fix the heavy metals in the solid residue while producing valuable oil and syngas products, with great advantages in terms of reduction, harmlessness and recycling. The common gasification technology and apparatus uses air as the gasification medium, and the main product is low-quality combustible gas including CO₂、O₂、CO、H₂Small amount of CH₄And a very small amount of C₂、C₃The calorific value of the gas (A) is generally 4-6MJ/Nm³And the utilization value except for combustion is not high. And the synthesis gas is H₂A mixture of two gases with a ratio of CO in the range of 2 to 3. The synthesis gas can be used to produce fuels or chemicals (such as diesel, methanol, ethanol), used to replace conventional fuel-fired boilers, and can also be used to generate electricity with gas turbines. However, in the prior art, the gasification technology is difficult to generate synthesis gas, or external steam is required to be used as a gasification medium to generate H₂CO as a mixture of main and other gases. Tar is generated in the process and the energy consumption is also large. Therefore, in the conventional gasification apparatus, the water content of the raw material for gasification needs to be strictly controlled, and is generally 25 to 30% or less. Otherwise the required air/fuel ratio increases due to the drying of the material, resulting in a lower quality of the final gas product. The Chinese patent application with the application number of 201610101851.4 discloses a method for preparing hydrogen-rich fuel gas by gasifying high-humidity sludge based on blast furnace slag waste heat recovery, which also utilizes the recovery of the moisture content of the sludge to achieve the purpose of gasifying the sludge to produce the hydrogen-rich fuel gas, but the high-humidity sludge needs to undergo two steps of drying and gasifying, the two steps need 2 heat sources, the system is complicated depending on the waste heat of liquid blast furnace slag, the form of a reactor cannot be provided, and the method can not be implemented when the method leaves a place with blast furnace slag. The utility model patent with application number CN201120530868.4 'a biomass pyrolysis gasification system', which aims at obtaining high-value fuel gas and directly burning the pyrolysis carbon to generate flue gasAs a drying heat source. However, the low-grade pyrolytic carbon has low combustion efficiency, usually needs to be supplemented with additional fuel, such as liquefied petroleum gas, and wastes sensible heat of the dry water vapor of the biomass.

Disclosure of Invention

The present invention has been made to solve the above problems, and an object of the present invention is to provide a gasification apparatus for producing a synthesis gas from a high moisture content organic material.

The invention provides a gasification device for producing synthesis gas from high moisture-containing organic materials, which is characterized by comprising the following components: the feeding device is used for adding the high-moisture organic material; one end of each pyrolysis reactor is connected with the feeding device, and the pyrolysis reactors are used for drying and pyrolyzing high-moisture organic materials; the gasification reactor is connected with one end of the pyrolysis reactor, which is far away from the feeding device, and is used for carrying out gasification reaction on pyrolysis reaction products; the solid particle separator is connected with the gasification reactor and is used for separating solid particles and gas generated by the gasification reaction; the residual coke box is connected with the gasification reactor and the solid particle separator and is used for receiving residual coke generated in the gasification reactor and the solid particle separator; a gas purification device connected with the solid particle separator and used for receiving and purifying the gas generated in the gasification reactor; and the combustion device is used for combusting gas to generate high-temperature flue gas, wherein the pyrolysis reactor is vertically arranged, the gasification reactor is horizontally arranged, and the two are arranged in an L shape.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the high moisture content organic material is an organic material with a water content of not more than 55 wt%.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the high moisture content organic material contains dolomite and/or nickel nitrate activator.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein, the upper part of the pyrolysis reactor is provided with a disturbance device for pushing and disturbing the materials in the pyrolysis reactor.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the working temperature of the pyrolysis reactor is 450-650 ℃.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the working temperature of the gasification reactor is 800-900 ℃.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the gas purification device is selected from any one of a Venturi type alkali scrubber with a defoaming measure, a spray type alkali scrubber with a defoaming measure and a sieve plate tower type alkali scrubber with a defoaming measure, and is combined with the active coke adsorption tower.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the gasification reactor is selected from a screw propelling type reactor or a rotary kiln reactor.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein, burner includes: a burner directly or indirectly communicated with the gas purification device, wherein the burner takes gas discharged from the gas purification device as fuel; and the combustion chamber is used for combusting gas and generating high-temperature flue gas, and the high-temperature flue gas is introduced into the outer layer and the inner side of the gasification reactor and the outer side of the pyrolysis reactor.

The gasification device for generating the synthesis gas by the high moisture content organic material provided by the invention can also have the following characteristics: wherein the solid particle separator is selected from any one of a cyclone dust collector, a foam metal filter and a ceramic filter.

Action and Effect of the invention

According to the gasification device of the high moisture content organic material, the carbon in the pyrolysis reactor in the device can continuously enter the gasification reactor, so that the gasification reactor can use the self-produced pyrolysis carbon as the catalyst, and the gasification reactor can be used immediately without inputting additional catalyst, therefore, the invention avoids the problem of unstable system operation caused by aging and invalidation of the catalyst, simultaneously fully utilizes the latent heat and volatile matters of water vapor and the sensible heat and chemical heat of the pyrolysis carbon, saves energy consumption, improves economy, and can conveniently add cheap activating agents such as dolomite into the high moisture content material as the catalyst under necessary conditions without specially arranging an expensive reactor for placing the catalyst.

Drawings

FIG. 1 is a schematic diagram of a gasification unit for producing synthesis gas from high moisture organic material according to examples 1-3 of the present invention;

FIG. 2 is a schematic diagram of a gasification apparatus for producing synthesis gas from high moisture content organic material according to example 4 of the present invention;

FIG. 3 is a schematic view of the construction of a perturbation device according to embodiments 1-2 of the present invention; and

FIG. 4 is a schematic view of the construction of a perturbation apparatus according to embodiments 3-5 of the present invention.

Detailed Description

In order to make the technical means, the creation features, the achievement purposes and the effects of the invention easy to understand, the invention is specifically described below by combining the embodiment and the attached drawings.

< example 1>

The water content of the dehydrated sludge obtained after the sewage treatment of a certain sewage treatment plant is 54 percent after being subjected to filter pressing by the heating plate frame, so that the cost of higher energy consumption, equipment investment and odor control caused by secondary drying is avoided, a traditional mode of burning after drying is not adopted, the gasification device for producing the synthesis gas by using the high-humidity organic matter material provided by the invention is selected to be recycled, and a gas product with better quality is obtained through heat treatment.

FIG. 1 is a schematic view showing the structure of a gasification apparatus for high moisture content organic materials according to examples 1 to 3 of the present invention.

As shown in fig. 1, the gasification apparatus for producing synthesis gas from high moisture content organic material provided in this embodiment includes a spiral feeding device 2, a pyrolysis reactor 3, a disturbance device interface 4, a heat preservation delivery pipe 5 for steam and volatile matter mixture, a gasification reactor 6, a solid particle separator 7, a gas purification device 8, a combustion device 10, a high temperature flue gas pipeline 11, a residual coke box 12, and a disturbance device 14.

The spiral feeding device 2 is connected with the pyrolysis reactor 3, and a smoke inlet of the spiral feeding device and a smoke outlet of the spiral feeding device are arranged on the outer side of the spiral feeding device.

The pyrolysis reactor 3 uses the mixed flue gas obtained by the high-temperature flue gas generated and directly introduced by the combustion device 10 (through the pipeline 11) and the high-temperature flue gas flowing in from the gasification reactor 6 as a heat source, the flue gas flowing out of the outer side of the pyrolysis reactor 3 continuously flows into a heating flue gas channel inlet arranged on the outer side of the spiral feeding and feeding device 2, and finally is discharged into a chimney from a flue gas outlet of the spiral feeding and feeding device 2.

The pyrolysis reactor 3 is vertically arranged and is connected with the input end of the gasification reactor 6 through the discharge end of the pyrolytic carbon and the heat preservation pipe 5 for conveying the mixture of the water vapor and the volatile matters.

The upper part of the air intake at the joint of the heat preservation pipe 5 of the mixture of the water vapor and the volatile matter and the upper part of the pyrolysis reactor 3 is covered, so that the material particles fed from the spiral feeding device 2 are prevented from being sucked into the heat preservation pipe 5.

FIG. 3 is a schematic view of the construction of a perturbation device according to embodiments 1-2 of the present invention.

As shown in fig. 3, a port 4 of a disturbing device is provided 125mm below the junction of the pyrolysis reactor 3 and the screw feeder 2. The perturbation device 14 is arranged inside the pyrolysis reactor 3 connected with the interface 4 of the perturbation device, and in the embodiment, the perturbation device 14 adopts a ring-shaped ladder perturbation plate which moves up and down. The downward movement amplitude of the scraping blade is consistent with the interval of the trapezoidal scraping blades which are annularly arranged, and the up-and-down movement can realize the cleaning of accumulated scale on the inner wall and promote the falling of materials.

The gasification reactor 6 is horizontally disposed to form an L-shape with the pyrolysis reactor 3. The output end of the gasification reactor 6 is connected with the solid particle separator 7 and the residual coke box 12, the outer side of the gasification reactor 6 is provided with a gasification reactor flue gas inlet and a gasification reactor flue gas outlet, and the gasification reactor flue gas inlet is connected with the combustion device 10. The flue gas outlet of the gasification reactor is connected with the flue gas inlet on the outer side of the pyrolysis reactor 3. In the present embodiment, the gasification reactor 6 is a screw propelling type reactor.

The solid particle separator 12 is a cyclone. The solid particle separator 7 is connected to the gasification reactor 6, the residual coke box 12, and the gas purification device 8, respectively.

The residual coke box 12 is connected to the gasification reactor 6 and to the solid particle separator 7.

The combustion apparatus 10 is composed of a burner and a combustion chamber; clean synthesis gas 9 discharged from the gasification purification device 8 is connected with a combustor through a pipeline, a combustion space is provided for the combustion chamber, and generated high-temperature flue gas is respectively connected with a flue gas inlet on the outer side of the gasification reactor 6, a flue gas inner inlet at the joint of the gasification reactor 6 and the pyrolysis reactor 3 and a flue gas inlet on the outer side of the lower part of the pyrolysis reactor 3 through pipelines 11.

The gas purification device 8 is a combination of a sieve plate tower type alkali liquor washer with a defoaming measure and an active coke absorption tower. The gas cleaning device 8 is connected to the solid particle separator 7.

In this example, the apparatus provided in this example was used to perform gasification by the following method:

the dewatered sludge 1 (with the water content of 54 wt%) which is not dried is added into a spiral feeding device 2, preheated by the flue gas 13 and sent into a pyrolysis reactor 3.

The vertical pyrolysis reactor 3 is adjusted by mixing high-temperature flue gas 11 directly fed from a combustion device 10 and flue gas introduced from a gasification reactor 6, the reactor 3 is heated to 550 ℃, materials are subjected to drying and pyrolysis reaction in the pyrolysis reactor 3 to generate water vapor, volatile matters and charcoal, a mixture of the water vapor and the volatile matters obtained by the pyrolysis reaction is fed into the gasification reactor 6 through a heat preservation pipe 5, the charcoal obtained by the pyrolysis reaction is also fed into the gasification reactor 6, and the mixture of the water vapor and the volatile matters is mixed in the gasification reactor 6; the temperature in the gasification reactor 6 is heated to 800 ℃ by high temperature flue gas. In this process, in order to further reduce and avoid the production of tar and at the same time increase the concentration of CO in the syngas produced, the high temperature flue gas produced by the combustion device 10 is also fed into the gasification reactor 6 via the flue gas duct 11A part for controlling the feeding amount to be 30% of the amount of the water vapor and the volatile matter so that the pyrolytic carbon is simultaneously coated with the water vapor, O₂And CO₂(from flue gas) are gasified together.

In the gasification reactor 6, carbon and contained oxides (e.g. SiO) from the pyrolysis char₂CaO, MgO and the like) and inorganic salt can play a role of a catalyst, so that the catalyst can be used as a cheap catalyst to catalyze the gasification reforming reaction among a mixture of high-temperature steam and volatile matters, pyrolysis carbon and high-temperature flue gas.

The synthesis gas enters a solid particle separator 7, the separated residual coke particles are guided into a residual coke box 12, the synthesis gas completely enters a gas purification device 8, and finally, part of the clean synthesis gas 9 is introduced into a combustor of a combustion device 10 to generate high-temperature flue gas, and most of the high-temperature flue gas is transported and utilized.

The content ratio of the target product synthesis gas obtained in this example to the product obtained by pure pyrolysis is shown in table 1.

TABLE 1 product content ratio control Table (vol.%)

As shown in the table, tar in the product obtained by gasification by using the device provided by the invention is eliminated; h in the obtained synthesis gas product₂The ratio is greatly increased, and CO₂Reduced ratio of H₂+ CO reached 76 vol.%.

< example 2>

The water content of the chicken manure produced by a certain chicken raising factory is 70 percent, the N content is high, a methane producing system through fermentation is unstable, and a pyrolysis gasification gas production scheme is changed. Mixing the straws according to the proportion of 30 percent, finally, the water content is 53.5 percent, and the dry base lower calorific value is 11.55 MJ/kg. The user wants to use the gasified fuel as heating gas.

FIG. 1 is a schematic diagram of a gasification apparatus for producing synthesis gas from high moisture organic material according to examples 1 to 3 of the present invention.

As shown in fig. 1, the gasification apparatus for producing synthesis gas from high moisture content organic material provided in this embodiment includes a spiral feeding device 2, a pyrolysis reactor 3, a disturbance device interface 4, a heat preservation delivery pipe 5 for steam and volatile matter mixture, a gasification reactor 6, a solid particle separator 7, a gas purification device 8, a combustion device 10, a high temperature flue gas pipeline 11, a residual coke box 12, and a disturbance device 14.

Wherein, spiral feed arrangement 2 is connected with pyrolytic reaction ware 3, and the outside is provided with spiral feed arrangement's heating flue gas entry and spiral feed arrangement's exhanst gas outlet.

The pyrolysis reactor 3 uses the mixed flue gas obtained by the high-temperature flue gas generated and directly introduced by the combustion device 10 (through the pipeline 11) and the high-temperature flue gas flowing in from the gasification reactor 6 as a heat source, the flue gas flowing out of the outer side of the pyrolysis reactor 3 continuously flows into the heating flue gas channel inlet arranged on the outer side of the spiral feeding device 2, and finally is discharged into a chimney from the flue gas outlet of the spiral feeding device.

The pyrolysis reactor 3 is vertically arranged and is L-shaped with the gasification reactor 4. Connected with the input end of a gasification reactor 6 through a heat preservation pipe 5 for conveying the mixture of the water vapor and the volatile matters. The upper part of the air intake at the joint of the heat preservation pipe 5 of the mixture of the water vapor and the volatile matter and the upper part of the pyrolysis reactor 3 is covered, so that the material particles fed from the spiral feeding device 2 are prevented from being sucked into the heat preservation pipe 5.

FIG. 3 is a schematic view of the construction of a perturbation device according to embodiments 1-2 of the present invention.

As shown in fig. 3, a port 4 of a disturbing device is provided 150mm below the junction of the pyrolysis reactor 3 and the screw feeder 2. The perturbation device 14 is arranged inside the pyrolysis reactor 3 connected with the interface 4 of the perturbation device, and in the embodiment, the perturbation device 14 adopts a ring-shaped ladder perturbation plate which moves up and down. The downward movement amplitude of the scraping blade is consistent with the interval of the trapezoidal scraping blades which are annularly arranged, and the up-and-down movement can realize the cleaning of accumulated scale on the inner wall and promote the falling of materials.

The gasification reactor 6 is arranged horizontally. The output end of the gasification reactor is connected with the solid particle separator 7 and the residual coke box 12, the outer side of the gasification reactor 6 is provided with a gasification reactor flue gas inlet and a gasification reactor flue gas outlet, and the gasification reactor flue gas inlet is connected with the combustion device 10. The flue gas outlet of the gasification reactor is connected with the flue gas inlet on the outer side of the pyrolysis reactor 3. In the present embodiment, the gasification reactor 6 is a screw propelling type reactor.

The solid particle separator 12 is a cyclone. The solid particle separator 7 is connected to the gasification reactor 6, the residual coke box 12, and the gas purification device 8, respectively.

The residual coke box 12 is connected to the gasification reactor 6 and to the solid particle separator 7.

The combustion apparatus 10 is composed of a burner and a combustion chamber; clean synthesis gas 9 discharged from the gasification purification device 8 is connected with a combustor through a pipeline, a combustion space is provided for the combustion chamber, and generated high-temperature flue gas is respectively connected with a flue gas inlet on the outer side of the gasification reactor 6, a flue gas inner inlet at the joint of the gasification reactor 6 and the pyrolysis reactor 3 and a flue gas inlet on the outer side of the lower part of the pyrolysis reactor 3 through pipelines 11.

The gas purification device 8 is a combination of a Venturi type alkali liquor washer with a defoaming measure and an active coke adsorption tower. The gas cleaning device 8 is connected to the solid particle separator 7.

In this example, the apparatus provided in this example was used to perform gasification by the following method:

the mixture 1 of chicken manure and straw (with a water content of 53.5 wt%) is added into a spiral feeding device 2, preheated by flue gas 13 and then sent into a pyrolysis reactor 3.

The vertical pyrolysis reactor 3 is adjusted by mixing high-temperature flue gas 11 directly fed from a combustion device 10 and flue gas introduced from a gasification reactor 6, the reactor 3 is heated to 550 ℃, materials are dried and pyrolyzed in the pyrolysis reactor 3 to generate water vapor, volatile matters and charcoal, the mixture of the water vapor and the volatile matters obtained by the pyrolysis reaction is fed into the gasification reactor 6 through a heat preservation pipe 5, and the charcoal obtained by the pyrolysis reaction is also fed into the gasification reactor 6 to be mixed and gasified with the mixture of the water vapor and the volatile matters; the temperature in the gasification reactor 6 is heated to 800 ℃ by high temperature flue gas. In this process, high temperature is generated from the combustion apparatus 10The flue gas is also fed into the gasification reactor 6 through a flue gas conveying pipeline 11, the feeding amount of the flue gas is controlled to be 18 percent of the amount of the water vapor and the volatile matter, so that the pyrolytic carbon is simultaneously treated by the water vapor and the CO₂And O₂Are gasified together.

In the gasification reactor 6, the alkali metal in the mixture of the biomass chicken manure and the straw has a good catalytic effect, and catalyzes the gasification and reforming reactions among the mixture of the steam and the volatile matter, the pyrolytic carbon and the high-temperature flue gas.

The synthesis gas enters a solid particle separator 7, the solid particle separator is selected from a foam metal filter, the separated residual coke particles are guided into a residual coke box 12, the synthesis gas completely enters a gas purification device 8, and finally 42% of the clean synthesis gas 9 is guided into a combustor of a combustion device 10 to generate high-temperature flue gas, and 58% of the clean synthesis gas is transported for use. If the traditional dry gasification process is adopted, the heat value of the generated fuel gas is only 2600KJ/kg of wet material, while the heat value of the recovered fuel gas is 3720KJ/kg of wet material and is as high as 10MJ/Nm by adopting the technology of the invention³The gas of (2). The residual coke is used as fertilizer additive.

< example 3>

The biogas residue produced by an anaerobic fermentation plant is dehydrated and dried primarily, the water content is 49 percent, and the dry base low calorific value is 11.2 MJ/kg. The user wants to realize the disposal of the biogas residues and recover energy from the biogas residues, so the device provided by the invention is used for gasification.

FIG. 1 is a schematic diagram of a gasification apparatus for producing synthesis gas from high moisture organic material according to examples 1 to 3 of the present invention.

As shown in fig. 1, the gasification apparatus for producing synthesis gas from high moisture content organic material provided in this embodiment includes a spiral feeding device 2, a pyrolysis reactor 3, a disturbance device interface 4, a heat preservation delivery pipe 5 for steam and volatile matter mixture, a gasification reactor 6, a solid particle separator 7, a gas purification device 8, a combustion device 10, a high temperature flue gas pipeline 11, a residual coke box 12, and a disturbance device 14.

The spiral feeding device 2 is connected with the pyrolysis reactor 3, and a heating flue gas inlet of the spiral feeding device and a flue gas outlet of the spiral feeding device are arranged on the outer side of the spiral feeding device.

The pyrolysis reactor 3 uses the mixed flue gas obtained by the high-temperature flue gas generated and directly introduced by the combustion device 10 (through the pipeline 11) and the high-temperature flue gas flowing in from the gasification reactor 6 as a heat source, the flue gas flowing out of the outer side of the pyrolysis reactor 3 continuously flows into the heating flue gas channel inlet arranged on the outer side of the spiral feeding device 2, and finally is discharged into a chimney from the flue gas outlet of the spiral feeding device.

The pyrolysis reactor 3 is vertically arranged and is L-shaped with the gasification reactor 4. Connected with the input end of a gasification reactor 6 through a heat preservation pipe 5 for conveying the mixture of the water vapor and the volatile matters.

The upper part of the air intake at the joint of the heat preservation pipe 5 of the mixture of the water vapor and the volatile matter and the upper part of the pyrolysis reactor 3 is covered, so that the material particles fed from the spiral feeding device 2 are prevented from being sucked into the heat preservation pipe 5.

FIG. 4 is a schematic view of the construction of a perturbation apparatus according to embodiments 3-5 of the present invention.

As shown in fig. 4, a port 4 of a disturbing device is provided 100mm below the junction of the pyrolysis reactor 3 and the screw feeder 2. The perturbation device 14 is arranged inside the pyrolysis reactor 3 connected to the perturbation device interface 4. In this embodiment, the disturbance device 14 is a straight-bar-shaped blade acting in a circumferential movement manner, one side of the blade is thin and the other side is thick, and when the blade moves along the circumferential direction, the thin side scrapes the inner wall of the pyrolysis reactor 3 to clean the scale and promote the falling of the material.

The gasification reactor 6 is horizontally arranged and is L-shaped with the pyrolysis reactor 3. The output end of the gasification reactor is connected with the solid particle separator 7 and the residual coke box 12, the outer side of the gasification reactor 6 is provided with a gasification reactor flue gas inlet and a gasification reactor flue gas outlet, and the gasification reactor flue gas inlet is connected with the combustion device 10. The flue gas outlet of the gasification reactor is connected with the flue gas inlet on the outer side of the pyrolysis reactor 3. In the present embodiment, the gasification reactor 6 is a screw propelling type reactor.

The solid particle separator 7 is a cyclone. The solid particle separator 7 is connected to the gasification reactor 6, the residual coke box 12, and the gas purification device 8, respectively.

The residual coke box 12 is connected to the gasification reactor 6 and to the solid particle separator 7.

The combustion apparatus 10 is composed of a burner and a combustion chamber; clean synthesis gas 9 discharged from the gasification purification device 8 is connected with a combustor through a pipeline, a combustion space is provided for the combustion chamber, and generated high-temperature flue gas is respectively connected with a flue gas inlet on the outer side of the gasification reactor 6, a flue gas inner inlet at the joint of the gasification reactor 6 and the pyrolysis reactor 3 and a flue gas inlet on the outer side of the lower part of the pyrolysis reactor 3 through pipelines 11.

The gas purification device 8 is a combination of a Venturi type alkali liquor washer with a defoaming measure and an active coke adsorption tower. The gas cleaning device 8 is connected to the solid particle separator 7.

In this example, the apparatus provided in this example was used to perform gasification by the following method:

adding the organic garbage anaerobic fermentation biogas residues 1 (with the water content of 49 wt%) which are not completely dried into a spiral feeding device 2, preheating the organic garbage anaerobic fermentation biogas residues through flue gas 13, and then sending the organic garbage anaerobic fermentation biogas residues into a pyrolysis reactor 3.

The vertical pyrolysis reactor 3 is adjusted by mixing high-temperature flue gas 11 directly fed from a combustion device 10 and flue gas introduced from a gasification reactor 6, the reactor 3 is heated to 450 ℃, materials are subjected to drying and pyrolysis reaction in the pyrolysis reactor 3 to generate water vapor, volatile matters and charcoal, the mixture of the water vapor and the volatile matters obtained by the pyrolysis reaction is fed into the gasification reactor 6 through a heat insulation pipe 5, and the charcoal obtained by the pyrolysis reaction is also fed into the gasification reactor 6 to be mixed and gasified with the mixture of the water vapor and the volatile matters; the temperature in the gasification reactor 6 is heated to 900 ℃ by high temperature flue gas. In the process, in order to further reduce and avoid the generation of tar and simultaneously improve the yield of the generated synthesis gas, high-temperature flue gas generated by the combustion device 10 is also fed into the gasification reactor 6 through the flue gas conveying pipeline 11, the feeding amount of the high-temperature flue gas is controlled to be 20% of the amount of water vapor and volatile matters, and the pyrolytic carbon is simultaneously subjected to the water vapor and the CO₂And O₂Are gasified together.

In the gasification reactor 6, the carbon is pyrolyzed by the oxides (e.g., SiO) contained in the biogas residue₂CaO, MgO, etc.), and the inorganic salt are relatively less and the catalytic action is insufficient, so the biogas residue 1 is mixed with the inorganic saltThe dolomite with 5 percent of dry weight can be used as a supplement of a cheap catalyst to catalyze the gasification reforming reaction among the mixture of high-temperature water vapor and volatile matters, the pyrolytic carbon and the high-temperature flue gas.

The synthesis gas enters a solid particle separator 7, the separated residual coke particles are guided into a residual coke box 12, the synthesis gas completely enters a gas purification device 8, and finally 62% of the clean synthesis gas 9 is introduced into a combustor of a combustion device 10 to generate high-temperature flue gas, and 38% of the high-temperature flue gas is transported and utilized. If the traditional drying gasification process is adopted, the generated fuel gas needs to be supplemented with external energy after being completely combusted.

< example 4>

The initial water content of certain household garbage is 50%. The dry basis heating value is 14.6MJ/kg, from which it is desired to obtain a better quality syngas.

FIG. 2 is a schematic diagram of a gasification apparatus for producing synthesis gas from high moisture content organic material according to example 4 of the present invention.

As shown in fig. 2, the gasification apparatus for producing synthesis gas from high moisture content organic material provided in this embodiment includes a spiral feeding device 2, a pyrolysis reactor 3, a disturbance device interface 4, a heat preservation delivery pipe 5 for steam and volatile matter mixture, a gasification reactor 6, a solid particle separator 7, a gas purification device 8, a combustion device 10, a high temperature flue gas pipeline 11, a residual coke box 12, and a disturbance device 14.

The spiral feeding device 2 is connected with the pyrolysis reactor 3, and a heating flue gas inlet of the spiral feeding device and a flue gas outlet of the spiral feeding device are arranged on the outer side of the spiral feeding device.

The pyrolysis reactor 3 uses the mixed flue gas obtained by the high-temperature flue gas generated and directly introduced by the combustion device 10 (through the pipeline 11) and the high-temperature flue gas flowing in from the gasification reactor 6 as a heat source, the flue gas flowing out of the outer side of the pyrolysis reactor 3 continuously flows into the heating flue gas channel inlet arranged on the outer side of the spiral feeding device 2, and finally is discharged into a chimney from the flue gas outlet of the spiral feeding device.

The pyrolysis reactor 3 is vertically arranged and is L-shaped with the gasification reactor 4. Connected with the input end of a gasification reactor 6 through a heat preservation pipe 5 for conveying the mixture of the water vapor and the volatile matters. The upper part of the air intake at the joint of the heat preservation pipe 5 of the mixture of the water vapor and the volatile matter and the upper part of the pyrolysis reactor 3 is covered, so that the material particles fed from the spiral feeding device 2 are prevented from being sucked into the heat preservation pipe 5.

FIG. 4 is a schematic view of the construction of a perturbation apparatus according to embodiments 3-5 of the present invention.

As shown in fig. 4, a port 4 of a disturbing device is provided 120mm below the junction of the pyrolysis reactor 3 and the screw feeder 2. The perturbation device 14 is arranged inside the pyrolysis reactor 3 connected to the perturbation device interface 4. In this embodiment, the disturbance device 14 is a straight-bar-shaped blade acting in a circumferential movement manner, one side of the blade is thin and the other side is thick, and when the blade moves along the circumferential direction, the thin side scrapes the inner wall of the pyrolysis reactor 3 to clean the scale and promote the falling of the material.

The gasification reactor 6 is horizontally arranged and adopts a rotary kiln type gasification reactor. The output end of the device is connected with a solid particle separator 7 and a residual coke box 12, the outer side of the gasification reactor 6 is provided with a flue gas inlet and a flue gas outlet, but the amount of the inflowing flue gas is small, and the flue gas is used for dynamic heat preservation instead of heating. The gasification reactor 6 is connected with a combustion device 10 at the flue gas inlet. The flue gas outlet of the gasification reactor is connected with the flue gas inlet on the outer side of the pyrolysis reactor 3. In this embodiment, the gasification reactor 6 is a rotary kiln reactor.

The solid particle separator 7 is a ceramic filter. The solid particle separator 7 is connected to the gasification reactor 6, the residual coke box 12, and the gas purification device 8, respectively.

The residual coke box 12 is connected to the gasification reactor 6 and to the solid particle separator 7.

The combustion apparatus 10 is composed of a burner and a combustion chamber; clean synthesis gas 9 discharged from the gasification purification device 8 is connected with a burner through a pipeline, a combustion space is provided for a combustion chamber, and generated high-temperature flue gas is connected with a flue gas inlet on the outer side of the gasification reactor 6, a flue gas inner inlet mainly fed into the joint of the gasification reactor 6 and the pyrolysis reactor 3 and a flue gas inlet on the outer side of the lower part of the pyrolysis reactor 3 through a pipeline 11 in a small amount.

The gas purification device 8 is a combination of a spray type alkali liquor washer with a defoaming measure and an active coke adsorption tower. The gas cleaning device 8 is connected to the solid particle separator 7.

In this example, the apparatus provided in this example was used to perform gasification by the following method:

the domestic waste 1 (water content of 50 wt%) which was only roughly crushed and separated large inorganic substances was fed to the feeding device 2, and the feeding device 2 was selected from shaftless twin screw. After a short preheating, it is fed into the pyrolysis reactor 3.

The vertical pyrolysis reactor 3 is mainly heated by high-temperature flue gas 11 directly fed from a combustion device 10, the reactor 3 is heated to 650 ℃, materials are dried and pyrolyzed in the pyrolysis reactor 3 to generate water vapor, volatile matters and charcoal, the mixture of the water vapor and the volatile matters obtained by the pyrolysis reaction is fed into a gasification reactor 6 through a heat preservation pipe 5, and the charcoal obtained by the pyrolysis reaction is also fed into the gasification reactor 6 to be mixed and gasified with the mixture of the water vapor and the volatile matters; the gasification reactor 6 is selected from rotary kiln reactors, and the temperature in the rotary kiln reactors is heated to about 850 ℃ by directly fed high-temperature flue gas. The amount of the flue gas directly fed into the gasification reactor 6 is controlled to be 38 percent of the amount of the water vapor and the volatile matter, so that the pyrolytic carbon is simultaneously treated by the water vapor and the CO₂And O₂Are gasified together.

In the gasification reactor 6, although the waste pyrolytic carbon contains oxides (e.g., SiO)₂CaO, MgO, etc.), in order to promote the catalytic action, nickel nitrate whose dry weight is 0.5% is mixed into the garbage 1 to improve its catalytic effect as an activator for pyrolysis of the garbage semicoke, catalyzing the gasification reforming reaction between the mixture of high-temperature steam and volatile matter, the pyrolysis char, and the high-temperature flue gas.

The synthesis gas enters a solid particle separator 7, the separated residual coke particles are guided into a residual coke box 12, the synthesis gas completely enters a gas purification device 8, and finally 32% of the clean synthesis gas 9 is introduced into a combustor of a combustion device 10 to generate high-temperature flue gas, and 68% of the high-temperature flue gas is transported and utilized.

The heat value of the obtained gas product can reach 13.8MJ/Nm through detection³Gas yield of 670m³T dry refuse, H₂The volume content of the + CO reaches 70 vol.%. And incineration of coalCompared with burning, the product with higher value is obtained, and the pollution and the harm of dangerous wastes such as dioxin, fly ash and the like are avoided.

< example 5>

The waste residue of a certain paper mill contains 42 percent of water, higher plastic content and larger volume. The dry basis heat value is 15.6 MJ/kg. A gasification plant for the production of synthesis gas using a high moisture content organic material of similar construction to that of example 1, with the difference that the number of pyrolysis reactors is 3.