CN210885959U - System for preparing synthesis gas by low-rank coal gasification reduction - Google Patents
System for preparing synthesis gas by low-rank coal gasification reduction Download PDFInfo
- Publication number
- CN210885959U CN210885959U CN201822020782.1U CN201822020782U CN210885959U CN 210885959 U CN210885959 U CN 210885959U CN 201822020782 U CN201822020782 U CN 201822020782U CN 210885959 U CN210885959 U CN 210885959U
- Authority
- CN
- China
- Prior art keywords
- gasification
- low
- coal
- rank coal
- reaction kettle
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Industrial Gases (AREA)
Abstract
The utility model discloses a system for low order coal gasification reduction preparation synthetic gas, including gasification reduction device, purifier, reforming conversion reactor, its characterized in that: the gasification reduction device is connected with the purification device through a gasification feeding device, and the reforming conversion reactor is connected with the purification device. The low-rank coal is treated by a gasification reduction device to obtain upgraded coalAnd the oil-gas mixture is purified by a system to obtain a mixture containing CO and H2And hydrocarbon, the mixed gas is processed by a partial hydrocarbon reforming converter to obtain a mixed gas containing CO and H2The gasification reduction device is used for carrying out chemical reaction of heating the dried low-rank coal under the condition of no oxygen or micro oxygen. The device in the utility model develops and utilizes the volatile components in the low-rank coal to prepare the coal rich in CO and H2The synthesis gas has high yield and low energy consumption.
Description
Technical Field
The utility model relates to a clean utilization technical field of coal material especially relates to a system of low order coal gasification reduction preparation synthetic gas.
Background
More than half of the coal reserves already explored in China are low-rank coals, and the volatile components in the low-rank coals are equivalent to 1000 hundred million tons of oil and gas resources. The low-rank coal mainly has the characteristics of high moisture and high volatility, flame is long and has smoke during combustion, the coalification degree is low, and typical coal types are brown coal and long flame coal. The coal-rich, oil-less and gas-deficient coal in China becomes a major subject of the clean coal technology at present by how to efficiently utilize low-rank coal. However, both combustion power generation and modern coal chemical utilization have extremely low comprehensive utilization efficiency due to the three characteristics of high water content, high ash content and low calorific value.
At present, the utilization mode of low-rank coal is mainly direct combustion or gasification. Direct combustion power generation is one of the most common utilization modes, and more than 90% of lignite in China is used for power station boilers and various industrial boilers according to incomplete statistics. The direct combustion of the low-rank coal not only wastes rich oil and gas resources contained in the coal and has low efficiency, but also pollutes the coalThe environment is polluted, so that a large amount of greenhouse gases such as SOx and NOx are easily generated, and severe weather environments such as acid rain are caused. The modern coal chemical technology uses coal gasification as a technical tap, and primary raw materials CO and H required by chemical synthesis are obtained by gasification2However, the coal gasification technology has not developed to date, and a mature large-scale commercial low-rank coal gasification technology has not yet been formed. In the prior art, low-rank coal gasification is used for preparing CO and H2Generally, low-rank coal is pyrolyzed to obtain raw coal gas and upgraded coal, and the pyrolysis is generally carried out in the presence of a large amount of oxygen (or air), wherein a part of coal is reacted with oxygen to supply heat and generate a large amount of CO2Due to CO2Can not burn, and belongs to ineffective gas; moreover, because of aerobic combustion, the nitrogen content in the crude gas is too high, the energy density of the crude gas is reduced, the calorific value of the crude gas is reduced, the crude gas cannot be used as a primary raw material for chemical synthesis, except for the return combustion, the mixed gas produced by pyrolysis has no other economic value, and the utilization rate of the coal raw material is low; and no related integrated equipment can utilize low-rank coal to continuously produce gas and can realize continuous large-scale production.
SUMMERY OF THE UTILITY MODEL
In view of the above, the present invention provides a system for preparing synthesis gas by low-rank coal gasification and reduction, which gasifies volatile components in low-rank coal to prepare mixed gas under oxygen-free or micro-oxygen condition, and reforms hydrocarbons in the mixed gas into CO and H2Increase CO and H in the mixed gas2High yield of synthesis gas.
In order to solve the technical problem, the utility model provides a following technical scheme:
the system for preparing the synthesis gas by low-rank coal gasification and reduction comprises a gasification reduction device, a purification device and a reforming conversion reactor, wherein the gasification reduction device is connected with the purification device through a gasification feeding device, and the reforming conversion reactor is connected with the purification device; the gasification reduction device comprises a horizontal reaction kettle capable of rotating by 360 degrees, a first heating mechanism and a driving mechanism for driving the horizontal reaction kettle to rotate, wherein the first heating mechanism is connected with the horizontal reaction kettle so as to heat low-rank coal in the horizontal reaction kettle; and a guide plate and a second heating mechanism are arranged in the horizontal reaction kettle, and the second heating branch pipe is connected with the first heating mechanism.
In one embodiment, the first heating mechanism comprises a heater and a heating box, the heater is connected with the heating box through a heating pipeline, the heating box is sleeved on the outer side of the horizontal reaction kettle and communicated with the horizontal reaction kettle through a first dynamic and static sealing device, the first heating mechanism is sleeved on the outer side of the horizontal reaction kettle, so that the first heating mechanism and the horizontal reaction kettle form two sets of relatively independent mechanisms, the first heating mechanism cannot rotate, and when the horizontal reaction kettle rotates under the power action of the driving mechanism, the joint of the heating box and the horizontal reaction kettle is in a sealing state through the first dynamic and static sealing device arranged between the horizontal reaction kettle and the heating box, the heating medium in the heating box is prevented from leaking outwards, the heat exchange between the horizontal reaction kettle and the heating mechanism is facilitated, and the heating efficiency is improved.
In one embodiment, the horizontal reaction kettle is provided with at least one stage, and can also be provided with multiple stages. When the multi-stage horizontal reaction kettle is adopted, the multi-stage horizontal reaction kettle mainly has the main functions of continuously gasifying solid matters (including gasified pulverized coal, solid impurities and the like) which cannot be gasified in the upper-stage horizontal reaction kettle and a certain amount of high-boiling-point oily matters such as similar asphalt and the like which cannot be gasified in a certain residence time, and the residence time is short enough to separate out or the temperature does not reach the polycondensation reaction conditions of phenolic compounds, aromatic hydrocarbon compounds and the like, thereby being beneficial to reducing volatile matters in upgraded coal and improving the quality of the upgraded coal.
In one embodiment, a plurality of wireless temperature controllers are further arranged inside the horizontal reaction kettle, and the wireless temperature controllers are used for monitoring the temperature in the horizontal reaction kettle and transmitting temperature signals to a background or an alarm device, so that workers can monitor the progress of the gasification reduction reaction in real time, and the controllability and the safety of the gasification reduction reaction are improved.
In one embodiment, the guide plate is of a single-spiral structure and/or a double-spiral structure, the guide plate is obliquely arranged and is of the spiral structure and/or the single-spiral structure, so that the produced upgraded coal is conveyed to a discharge port and discharged while the low-rank coal in the horizontal reaction kettle is continuously gasified and reduced, and then the gasification and reduction reaction can be more fully performed in the process of conveying the low-rank coal through the guide plate by matching with the rotation of the horizontal reaction kettle.
In one embodiment, the upper end of the gasification feeding device is communicated with the purification device, so that the oil-gas mixture generated by the gasification reduction device enters the upper end of the gasification feeding device through the feeding hole and then enters the purification device.
In one embodiment, the gasification feeding device is in a cylinder shape, and the gasification feeding device is connected with the gasification reduction device through a metal compensator and a second dynamic and static sealing device, so that the sealing performance and the connection stability between the gasification feeding device and the gasification reduction device are increased.
In one embodiment, a helical blade is arranged in the gasification feeding device, the cross section of the helical blade is not larger than the inner diameter cross section of the gasification feeding device, the helical blade is used for conveying low-rank coal through the helical blade, gasifying the low-rank coal and dispersing the low-rank coal into suspended uniform particles, and then enabling the suspended uniform particles to enter a feeding hole of the gasification reduction device, and meanwhile, an oil-gas mixture generated by the gasification reduction device enters the upper end of the gasification feeding device through the feeding hole and then enters the purification device.
In one embodiment, the purification device comprises a dust removal device, a tar removal device and a desulfurization device, and the dust removal device, the tar removal device and the desulfurization device are connected in sequence and used for removing dust, coal tar, water vapor and sulfur-containing compounds of the oil-gas mixture to obtain a product containing CO and H2And mixed gases such as hydrocarbons.
The utility model discloses profitable effect: gasifying volatile components in low-rank coal under the condition of no oxygen or micro oxygen to prepare mixed gas, and reforming and converting hydrocarbons in the mixed gas into CO and H2Increase CO and H in the mixed gas2The content of the synthetic gas is high, and the heat value is high; wherein the utility model has simple device, easy operation and moreThe method has the advantages of low operation cost, low process degree and high safety for the existing equipment, ensures that the synthesis gas can be prepared safely and efficiently, and can reasonably and fully utilize the products generated by the low-rank coal in the whole process through the arrangement design among devices.
Drawings
FIG. 1 is a schematic structural diagram of a device for preparing synthesis gas by low-rank coal gasification reduction in an embodiment of the invention;
FIG. 2 is a schematic structural view of a gasification reduction apparatus according to an embodiment of the present invention;
FIG. 3 is a front partial sectional view of a structure of a gasification reduction apparatus according to an embodiment of the present invention;
FIG. 4 is a schematic view of a gasification feed apparatus according to an embodiment of the present invention.
In the figure: 1. the device comprises a horizontal reaction kettle, 2, a feed inlet, 3, a discharge outlet, 4, a driving mechanism, 41, a toothed ring, 42, a riding wheel, 43, a first motor, 44, a transmission gear, 5, a first heating mechanism, 51, a heater, 52, a heating box, 53, a heating pipeline, 54, a heating air outlet, 6, a second heating mechanism, 7, a guide plate, 9, a first dynamic and static sealing device, 10, a gasification reduction device, a gasification feed device, 151, a metal compensator, 152, a second dynamic and static sealing device, 153, a second motor, 154, a helical blade, 200, a purifying device, 210, a dust removal device, 220, a tar removal device, 230, a desulfurization device, 300 and a reforming conversion reactor.
Detailed Description
The present invention will be further described with reference to the following specific embodiments, but the present invention is not limited to these specific embodiments. It will be recognized by those skilled in the art that the present invention encompasses all alternatives, modifications, and equivalents as may be included within the scope of the claims.
In the utility model, if not, the adopted raw materials and equipment can be purchased from the market or commonly used in the field. The methods in the following examples are conventional in the art unless otherwise specified.
The utility model discloses a raw materials low order coal can be fine coal also can be lump coal, when the low order coal adopted the lump coal, can be through crushing, screening processing in order to obtain the less fine coal of granularity to the bold coal. When the low-rank coal adopts the pulverized coal as a raw material, on one hand, the pulverized coal does not need to be crushed and screened, so that the process steps are saved, the heating area is large during drying, the drying efficiency is high, on the other hand, the pulverized coal is low in price compared with lump coal, and the pulverized coal with the granularity smaller than 20mm is selected as the common pulverized coal. Further preferably, pulverized coal having a particle size of less than 6mm is used. When the raw material low-rank coal is pulverized coal, the low-rank coal can directly enter the drying device 100 through the conveying device to be dried.
The utility model provides a system for low order coal gasification reduction preparation synthetic gas.
Referring to fig. 1, an apparatus for producing synthesis gas by low-rank coal gasification and reduction comprises a gasification reduction apparatus 10, a purification apparatus 200, and a reforming conversion reactor 300, wherein the gasification reduction apparatus 10 is connected to the purification apparatus 200 through a gasification feeding apparatus 150, and the reforming conversion reactor 300 is connected to the purification apparatus 200;
wherein, the gasification reduction device 10 is used for converting volatile components, coal tar and the like in low-rank coal into gaseous state by low-valence coal gasification reduction to obtain high-temperature oil-gas mixture and upgraded coal with a certain temperature, and the purification device 200 is used for removing dust, coal tar, water vapor and sulfur-containing compounds in the oil-gas mixture to obtain the upgraded coal containing CO and H2And hydrocarbons, the reforming conversion reactor 300 is used for reforming and converting most of the hydrocarbons in the mixed gas into CO and H2And the reformed and converted mixed gas is the first synthesis gas.
A gasification feeding device:
as shown in fig. 4, the gasification feeding device 150 includes a gasification feeding chamber and a spiral blade 154 disposed in the gasification feeding chamber, and a second motor 153 for driving the spiral blade to rotate, and the cross section of the spiral blade 154 is not larger than the inner diameter cross section of the gasification feeding chamber.
The gasification feeding device 150 may be disposed at the discharge port 3 or the feed port 2 of the gasification reduction device 10. The upper end of the gasification feeding device 150 is connected with the purification device 200, when the gasification feeding device 150 is arranged at the discharge port 3 of the gasification reduction device 10, low-rank coal enters the gasification reduction device 10 through the conveying device, an oil-gas mixture generated by the gasification reduction device 10 firstly enters the upper end of the gasification feeding device 150 through the discharge port 3 and then enters the purification device 200, upgraded coal produced in the gasification reduction device 10 is conveyed to the next device from the discharge port 3 through the gasification feeding device 150, and the gasification feeding device 150 is only an oil-gas mixture conveying channel and an upgraded coal conveying device after gasification reduction reaction.
When the gasification feeding device 150 is arranged at the feeding port 2 of the gasification reduction device 10, on one hand, low-rank coal is conveyed by the gasification feeding device 150, gasified and dispersed into suspended uniform particles, and then enters the feeding port 2 of the gasification reduction device 10, meanwhile, an oil-gas mixture generated by the gasification reduction device 10 enters the upper end of the gasification feeding device 150 through the feeding port 2 and then enters the purification device 200, and the high-temperature oil-gas mixture and the low-rank coal are subjected to heat exchange in the gasification feeding device 150, so that the temperature of the low-rank coal entering the gasification reduction device 10 is favorably increased, therefore, the gasification feeding device 150 is a conveying device for dried materials, and the low-rank coal is in the form of dispersed uniform particles in the gasification reduction device and is uniformly heated so as to be conveniently; but also improves the temperature of the low-rank coal entering the gasification reduction device 1. Therefore, the gasification feed device 150 is preferably arranged at the feed opening 2 of the gasification reduction device 10.
Further, in order to increase the sealing performance, a metal compensator 151 and a dynamic and static sealing device 152 are arranged outside the gasification feeding cavity and the feeding port 2 of the horizontal reaction kettle 1 to increase the sealing performance and the connection stability between the gasification feeding device 150 and the horizontal reaction kettle.
Gasification reduction device
The gasification reduction device is a chemical reaction process for heating low-rank coal under the condition of no oxygen or micro oxygen. Conveying the low-rank coal to a gasification reduction device, heating by heating media such as flue gas and the like, adding other substances such as additives and the like in the reaction process, generally performing a complex chemical reaction process at the temperature of 350-800 ℃ and the pressure of less than or equal to 30Kpa to obtain solid carbon and a high-temperature oil-gas mixtureWherein the solid carbon is upgraded coal, and the volatile content in the upgraded coal is 3-8%. The high-temperature oil-gas mixture contains CO and H2、CO2Hydrocarbon, coal tar, dust, sulfur compounds, and the like.
As shown in fig. 1-3, low-rank coal enters a gasification reduction device 10 through a conveying device, the gasification reduction device 10 comprises a horizontal reaction kettle 1 capable of rotating for 360 degrees, a first heating mechanism 5 and a driving mechanism 4 for driving the horizontal reaction kettle 1 to rotate, and the first heating mechanism 5 is connected with the horizontal reaction kettle 1 to heat the low-rank coal in the horizontal reaction kettle 1; the horizontal reaction kettle 1 is provided with a discharge port 3 and a feed port 2, low-rank coal enters from the feed port 2 and is output from the discharge port 3 through a guide plate arranged in the horizontal reaction kettle 1, and an oil-gas mixture generated in the horizontal reaction kettle 1 is discharged from the feed port 2.
The driving mechanism 4 includes a gear ring 41 disposed on the outer peripheral surface of one end of the horizontal reactor 1, a supporting roller 42 engaged with the gear ring 41, a transmission gear 44, and a first motor 43, where the first motor 43 drives the transmission gear 44 to rotate, and further drives the supporting roller 42 to rotate, so as to drive the gear ring 41 and the horizontal reactor 1 to rotate again, and it should be noted here that the driving mechanism 4 may also be another device as long as the same technical effect can be achieved.
The rotation of horizontal reation kettle 1 is 360 rotations to can be so that its inside low order coal is in the rotation state constantly, with the heated area of the heating medium that increases low order coal and first heating mechanism 5 provided, be favorable to accelerating low order coal gasification reduction reaction, wherein, first heating mechanism 5 carries out the gasification reduction of continuous heating to the low order coal in horizontal reation kettle 1 through the transmission heating medium, make the low order coal can furthest produce oil gas mixture and upgrade coal, thereby produce the most coal energy value of utilizing when utilizing fewest heating resources.
The first heating mechanism 5 comprises a heater 51 and a heating box 52, wherein the heater 51 is connected with the heating box 52 through a heating pipeline 53, and the heating box 52 is sleeved outside the horizontal reaction kettle 1 and is connected with the horizontal reaction kettle 1 through a dynamic and static sealing device 9. By adopting the structural design, the heating medium is prevented from leaking to improve the energy utilization rate, and finally the heating medium is discharged through the heating gas outlet 54, so that the first heating mechanism 5 and the horizontal reaction kettle 1 form two sets of relatively independent mechanisms, therefore, the occupied space of the whole device can be better arranged according to actual production scenes, meanwhile, the heating medium can be enabled to perform continuous heat exchange with low-rank coal in the horizontal reaction kettle 1, in order to increase the stability of the first heating mechanism 5, the first heating mechanism 5 can be fixedly arranged, for example, the first heating mechanism 5 can be fixed on the ground or a support. Further preferably, a heat insulating device such as heat insulating cotton is provided outside the heating box 52 to prevent the temperature of the first heating means 5 from decreasing. Further preferably, the heating pipes 53 may be multiple, and the heating medium is introduced into the multiple heating pipes 53 from different positions of the bedroom reactor 1, so as to accelerate the rate of the gasification reduction reaction.
Wherein the guide plate 7 is of a single-spiral structure and/or a double-spiral structure, the guide plate 7 which is obliquely arranged and is of a spiral structure and/or a single-spiral structure is arranged, the low-rank coal in the horizontal reaction kettle 1 is continuously gasified and reduced, the generated upgraded coal is conveyed to the discharge port 3 to be discharged, and then the rotation of the horizontal reaction kettle 1 is matched, so that the low-rank coal can be more fully subjected to gasification reduction reaction in the process of being conveyed by the guide plate 7, wherein the guide plate 7 is divided into a guide steel plate and a guide stainless steel plate, can adopt a single spiral structure or a double spiral structure, can also adopt a single and double combined spiral guide structure for guide, adopts the structural design, in the rotating process of the horizontal reaction kettle 1, the low-rank coal in the horizontal reaction kettle 1 moves to the discharge port 3 under the action of the spiral guide plate 7, and the discharge of the quality-improved coal of the product after the gasification reduction reaction in the horizontal reaction kettle 1 is accelerated.
The gasification reduction device 10 is set to be at least one stage or multistage, and can be provided with a second-stage horizontal reaction kettle 1 as required to perform more sufficient and complete gasification reduction on the low-rank coal, and simultaneously can also increase the feeding amount of the gasification reduced low-rank coal, and meanwhile, the 360-degree rotatable horizontal reaction kettle can enable the low-rank coal inside the horizontal reaction kettle to be in a motion state all the time so as to be heated more comprehensively and uniformly. Wherein, the utility model discloses well preferred horizontal reation kettle includes one-level horizontal reation kettle and second grade horizontal reation kettle, connect through sealed conveyor between one-level horizontal reation kettle and the second grade horizontal reation kettle, conveyor here is gasification feed arrangement 150. The method comprises the following steps that first-order gas and first-order solid are obtained after low-rank coal reacts in a first-order horizontal reaction kettle, the first-order gas enters a subsequent purification device 200 from the upper end of a gasification feeding device 150, the first-order solid enters a second-order horizontal reaction kettle through the gasification feeding device 150 to react continuously to obtain second-order gas and second-order solid, the second-order solid is upgraded coal, the second-order gas enters the subsequent purification device 200 from the upper end of the gasification feeding device 150, and preferably, the capacity of the second-order horizontal reaction kettle is smaller than that of the first-order horizontal. After the low order coal passes through the gasification reduction of one-level horizontal reation kettle, can produce a certain amount of oil-gas mixture, the volume of remaining solid coal will significantly reduce this moment, after reducing the capacity of the horizontal reation kettle of second grade so, can satisfy the regasification reduction of remaining solid coal more better, consequently such design, more reasonable and abundant the capacity of having utilized the device to the occupation of land space has been saved, the rationality of device has been improved.
Wherein, after the low-rank coal is gasified and reduced by the first-stage horizontal reaction kettle, the volatile content in the upgraded coal is 8-15 wt%, and after the low-rank coal is gasified and reduced by the second-stage horizontal reaction kettle, the volatile content in the upgraded coal is 3-8 wt%. The main factors are related to the reaction temperature and the type of the low-rank coal, and are determined by the reaction temperature.
Wherein, horizontal reation kettle 1 is inside to be equipped with second heating mechanism 6 for horizontal reation kettle 1 is inside to be heated evenly. Further, the second heating mechanism 6 uniformly heats the low-rank coal in the horizontal reaction kettle by controlling the flow rate, temperature, pressure and the like of heating media such as flue gas and the like; the first heating mechanism 5 heats the low-rank coal from the outside of the horizontal reaction kettle.
Thereby realize the flow of heating medium inside and outside horizontal reation kettle 1 for the low order coal can contact a large amount of heats along with horizontal reation kettle 1 is rotatory simultaneously, with better gasification reduction reaction that carries on, improves gasification reduction reaction's efficiency and speed.
Wherein, horizontal reation kettle 1 is inside still to be equipped with a plurality of wireless temperature controller. The wireless temperature controller is used for monitoring the temperature in the horizontal reaction kettle 1 and transmitting a temperature signal to the background or the alarm device, so that workers can monitor the proceeding condition of the gasification reduction reaction in real time, and the controllability of the gasification reduction reaction and the safety of the reaction are improved. When the temperature of the discharge port 3 of the equipment does not reach the designated temperature, the temperature sensor transmits a signal to a computer and an alarm device to remind workers, which means that the product does not reach the qualified requirement, at the moment, the horizontal reaction kettle 1 can rotate reversely, so that solid materials which are fast to the discharge port 3 enter the horizontal reaction kettle 1 again to fully react, the retention time is prolonged, meanwhile, the heating is continued, the reverse rotation time of the horizontal reaction kettle 1 is unequal to 30min-4h, then the horizontal reaction kettle 1 rotates forwards, when the solid materials enter the discharge port 3, whether the temperature sensor alarms or not is observed, if the alarm is given, the horizontal reaction kettle 1 rotates backwards again, and the operation is repeated, and the qualified product is ensured to be off line. If the temperature sensor shows that the temperature reaches the standard, the low-rank coal enters the discharge port 3 and is conveyed to the next procedure through the conveying device.
Purifying device
The purification device 200 comprises a dust removal device 210, a tar removal device 220 and a desulfurization device 230, namely, the oil-gas mixture is sequentially treated by the dust removal device 210, the tar removal device 220 and the desulfurization device 230 to obtain the gas mixture containing CO and H2And a hydrocarbon-based mixed gas. The high-temperature oil-gas mixture contains a large amount of dust, coal tar, water vapor, sulfur-containing compounds and the like; the dust removal device 210 is used for removing dust firstly, so that the temperature of an oil-gas mixture is prevented from being reduced in the dust removal process, coal tar, water vapor and the like are condensed into liquid and are adhered with a large amount of dust to cause subsequent pipeline blockage, and the dust removal effect is prevented from being reduced; then, a large amount of tar and water vapor are removed by using the tar removing device 220, so that the problems of blockage of the pipeline, carbon deposition and the like caused by cooling and adhesion of the tar in the pipeline are prevented; finally, the residual gas treated by the tar removing device 220 is treated by a desulfurizing device 230 to remove sulfur-containing compounds, so that the sulfur-containing compounds are prevented from causing catalyst poisoning in the subsequent process, and the catalyst is collectedThe device can remove impurity gas and solid so as to obtain purified mixed gas, the impurity of the mixed gas is less, the subsequent process treatment is convenient, and the stability of subsequent equipment is ensured.
As shown in fig. 1, the dust removing device 210 is connected to the upper end of the gasification feeding device 150, that is, the high-temperature oil-gas mixture enters the dust removing device 210 to remove a large amount of solid impurities such as dust, then enters the tar removing device 220 through the gas outlet of the dust removing device 210 to remove a large amount of coal tar, and then enters the desulfurization device 230 to remove a large amount of sulfur-containing compounds, in order to further optimize the device, an electric tar capturing device may be added behind the desulfurization device 230 to capture a small amount of tar; still further preferably, a hydrogenation apparatus, a denitration apparatus, and a dechlorination apparatus may be additionally provided to realize further purification.
When two-stage gasification reduction devices are adopted, preferably, each stage of gasification reduction device is respectively and sequentially connected with the respective dust removal device 210, the tar removal device 220 and the desulfurization device 230, preferably, each stage of gasification reduction device 1 is firstly connected with the respective dust removal device 210, and then each stage of dust removal device 210 is sequentially connected with the same set of tar removal device 220 and desulfurization device 230, so that equipment is saved, and the production cost expenditure is reduced.
The dust removing device 210 includes one or more of a gravity dust removing device, a cyclone separating device, and an electric dust removing device. Further preferably, the dust collector 210 may be insulated with heat insulation cotton to prevent the temperature of the oil-gas mixture from dropping too fast, and if the temperature drops too fast, the heavy oil and the like may easily form liquid, which may cause the coal tar to adhere to the dust collector and cause blockage.
The tar removing device 220 mainly comprises a spray cooling tower, a diesel cooler, a gasoline cooler, an oil-water separator and other equipment, so that high-temperature oil gas is cooled to coal tar with similar gasoline and diesel boiling points according to different grades and qualities of the boiling points. The spray cooling tower uses the cooled industrial wastewater or cooling medium such as heavy oil to cool the tar and the water vapor in the high-temperature oil-gas mixture and then convert the tar and the water vapor into a liquid oil-water mixture, so that the oil and the water are separated from the residual gas, and the residual gas is discharged from the gas outlet of the spray cooling tower, enters the subsequent equipment, and then enters the desulfurization device 230 for treatment.
After further optimization, the gas treated by the tar removing device 220 enters the desulfurizing device 230 for desulfurization. The desulfurization apparatus 230 can be broadly classified into two methods, dry desulfurization, which is widely used in the iron oxide method and the activated carbon method, and wet desulfurization, which is typified by the arsenic-alkali method, ADA, modified ADA, and tannin extract method. In the wet desulfurization technology of producer gas, tannin extract desulfurization method is widely applied. It uses soda as absorbent, tannin extract as oxygen carrier and NaVO2Is an oxidizing agent. The whole desulfurization and regeneration process of wet tannin extract desulfurization is a continuous online process, desulfurization and regeneration are carried out simultaneously, and a standby desulfurizing tower is not required to be arranged; the desulfurization and purification degree of the coal gas can be adjusted and timely controlled by adjusting the solution ratio according to the needs of enterprises, and H in the purified coal gas2The S content is stable. The utility model discloses in prefer wet-type tannin extract method desulfurization, desulphurization unit 230 is the wet flue gas desulfurization tower.
It is further preferred that the mixed gas is compressed by a compression device and then enters the reforming conversion reactor 300.
The mixed gas obtained after the treatment of the purification device enters a reforming conversion reactor 300, and the mixed gas is reformed and converted by partial hydrocarbon, namely, all components of the gas in the mixed gas are not separated, and partial hydrocarbon is directly reformed and converted into CO and H2Because the reforming conversion is only intended to convert hydrocarbons to CO and H2The first synthesis gas is obtained, and the mixed gas contains a part of CO and H2, so that the hydrocarbon does not need to be separated from the mixed gas and then reformed and converted, and the operation saves process steps and is high in economic benefit.
The reforming converter 300 mainly includes partial catalytic oxidation, steam catalytic reforming conversion, and non-catalytic reforming conversion. The catalyst is needed for partial catalytic oxidation and steam catalytic reforming conversion, the catalyst for reforming conversion process is mostly a load type catalyst, and the active components are mainly non-metals such as Ni, Co, Fe, Cu and the like and noble metals such as Rh, Ru, Pt and the like. Reforming conversion generally requires heat supply and can be performed directlyHeating or indirect heating. CO and H in the first syngas2The source of the (C) is two parts, one part is CO and H obtained by catalytic conversion of partial hydrocarbons in the mixed gas2The other part is original H in the mixed gas2And CO.
The partial catalytic oxidation adopts oxygen and partial hydrocarbon to burn and directly supply heat, so that the reaction temperature reaches 850-1300 ℃, and partial hydrocarbon in the mixed gas reacts with steam to generate CO and H under the action of the catalyst2(ii) a When the steam catalytic reforming conversion is carried out, external heat supply is adopted, the temperature is up to 850-1200 ℃, and partial hydrocarbons in the mixed gas react with steam to generate CO and H under the action of a catalyst2(ii) a The main reaction mechanism of the two methods is:
(1)CmHn+mH2O＝mCO+1/2(n+2m)H2main reaction, endothermic reaction
(2)CO+H2O＝CO2+H2Side reactions, endothermic reactions
With CH4For example, the main reaction equation is CH4+H2O→CO+3H2Generation of H2The molar ratio of CO to CO is 3:1, and the ratio is large, so that the preparation of the first synthesis gas is very favorable.
The non-catalytic reforming conversion reforming does not need a catalyst, and the main reaction mechanism is as follows: CH (CH)4+1/2O2→CO+2H2Generation of H2And CO in a 2:1 molar ratio, facilitating the preparation of the first synthesis gas. Hydrocarbons other than methane with methane and O2The reaction mechanism of (3) is similar.
The reforming conversion reactor 300 is provided with an air inlet and an air outlet, and the reforming conversion reactor 300 comprises partial catalytic oxidation conversion, steam catalytic reforming conversion and non-catalytic reforming conversion. When partial catalytic oxidation conversion is adopted, oxygen and steam are introduced into a reforming conversion reactor to be combusted for heat supply, and under the action of a catalyst, hydrocarbons such as methane and the like in the mixed gas react with the steam to generate a mixture mainly containing CO and H2The first synthesis gas of (a); when the steam catalytic reforming conversion is adopted, an external heat supply is needed to heat the reforming conversion reactor, and water vapor is led to pass through the air inletIntroducing the gas into a reforming conversion reactor, and under the action of a catalyst, discharging gas from a gas outlet of the reforming conversion reactor, namely the gas containing CO and H2The first synthesis gas of (a); when non-catalytic reforming conversion is adopted, an external heat supply heats the reforming conversion reactor, oxygen is introduced into the reforming conversion reactor to react with hydrocarbons, and the obtained product mainly contains CO and H2The first synthesis gas of (a).
Table 1: the range value of the volume percentage of each component in the mixed gas before reforming conversion is as follows:
| components | H2 | Comprising CH4Of (2) | CO | CO2 | Others |
| Content (wt.) | 15-45％ | 10-52％ | 5-25％ | 5-25％ | 0.1-10％ |
The other component is N2And steam, etc., the volume percentages of the components in the mixed gas before reforming conversion are integrated to 100%.
Table 2: the range value of the volume percentage of each component in the mixed gas after reforming conversion is as follows:
| components | H2 | Comprising CH4Of (2) | CO | CO2 | Others |
| Content (wt.) | 30-70％ | 1-5％ | 10-30％ | 3-35％ | 0.1-10％ |
The other component is N2And steam, etc., the volume percentage of each component in the mixed gas after reforming conversion is integrated to be 100%.
Because the gasification reduction device in-process does not add the foreign matter basically, according to the law of conservation of mass, the weight of the obtained mist is 15 ~ 50% of low order coal volatiles after low order coal is handled through drying device, gasification reduction device and purifier, can prove from this to utilize the utility model provides a device makes the gas in the low order coal basically gasified completely, and the output of the mist of obtaining is high. As can be seen from tables 1 and 2, the hydrocarbons in the mixed gas are treated by the reformer 300The volume ratio of the first synthetic gas to the second synthetic gas is reduced from 10-52% to 1-5%, the reformed and converted mixed gas is the first synthetic gas, and H in the first synthetic gas2And the volume ratio percentage of CO is greatly improved.
The above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention in its corresponding aspects.
Claims (9)
1. The system for preparing the synthesis gas by low-rank coal gasification and reduction comprises a gasification reduction device (10), a purification device (200) and a reforming conversion reactor (300), and is characterized in that: the gasification reduction device (10) is connected with the purification device (200) through a gasification feeding device (150), and the reforming conversion reactor (300) is connected with the purification device (200);
the gasification reduction device (10) comprises a horizontal reaction kettle (1) capable of rotating by 360 degrees, a first heating mechanism (5) and a driving mechanism (4) for driving the horizontal reaction kettle (1) to rotate, wherein the first heating mechanism (5) is connected with the horizontal reaction kettle (1) to heat low-rank coal in the horizontal reaction kettle (1); a guide plate (7) and a second heating mechanism (6) are arranged in the horizontal reaction kettle (1), and the second heating mechanism (6) is connected with the first heating mechanism (5).
2. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the first heating mechanism (5) comprises a heater (51) and a heating box (52), wherein the heater (51) is connected with the heating box (52) through a heating pipeline (53).
3. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the horizontal reaction kettle (1) is arranged to be at least one stage.
4. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the horizontal reaction kettle (1) is also internally provided with a plurality of wireless temperature controllers.
5. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the guide plate (7) is of a single spiral structure and/or a double spiral structure.
6. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the upper end of the gasification feeding device (150) is communicated with the purification device (200).
7. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the gasification feeding device (150) is in a cylinder shape, and the gasification feeding device (150) is connected with the gasification reduction device (10) through a metal compensator (151) and a second dynamic and static sealing device (152).
8. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 7, wherein: a spiral blade (154) is arranged in the gasification feeding device (150), and the cross section of the spiral blade (154) is not larger than the inner diameter cross section of the gasification feeding device (150).
9. The system for preparing the synthesis gas by low-rank coal gasification and reduction according to claim 1, wherein: the purification device (200) comprises a dust removal device (210), a tar removal device (220) and a desulfurization device (230), and the dust removal device (210), the tar removal device (220) and the desulfurization device (230) are sequentially connected.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2018220067277 | 2018-11-30 | ||
| CN201822006727 | 2018-11-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210885959U true CN210885959U (en) | 2020-06-30 |
Family
ID=71333174
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201822020782.1U Active CN210885959U (en) | 2018-11-30 | 2018-12-04 | System for preparing synthesis gas by low-rank coal gasification reduction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210885959U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920819A (en) * | 2021-01-25 | 2021-06-08 | 河北化工医药职业技术学院 | Horizontal rotary pyrolysis reaction kettle for household garbage |
-
2018
- 2018-12-04 CN CN201822020782.1U patent/CN210885959U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112920819A (en) * | 2021-01-25 | 2021-06-08 | 河北化工医药职业技术学院 | Horizontal rotary pyrolysis reaction kettle for household garbage |
| CN112920819B (en) * | 2021-01-25 | 2021-07-16 | 河北化工医药职业技术学院 | Horizontal rotary pyrolysis reaction kettle for household garbage |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109652139A (en) | A kind of method and system preparing synthesis gas using volatile matter in low-order coal and waste water | |
| CN101100621A (en) | Method and device for preparing biomass hydrogen-rich combustion gas | |
| CN101434879A (en) | Method for preparing methyl alcohol synthesis gas and compressed natural gas from coke oven gas and coal | |
| CN110055104A (en) | A kind of method that the utilization of low-order coal sub-prime prepares natural gas | |
| CN108504394B (en) | Catalytic pyrolysis-gasification integrated reaction device and method | |
| CN103045307A (en) | Pyrolysis and gasification method and device for preparing tar-free hydrogen-rich gas | |
| CN111378512A (en) | Method and system for preparing synthesis gas by biomass pyrolysis and gasification | |
| CN104498117A (en) | Method and device for preparing methane-enriched gas from carbon-containing raw materials | |
| CN101239702A (en) | High temperature coke oven crude gas hydrogen generating system device and technique | |
| CN104910969B (en) | A kind of brown coal hydrogasification system and method | |
| CN210885959U (en) | System for preparing synthesis gas by low-rank coal gasification reduction | |
| CN107557075B (en) | Biomass indirect liquefaction synthetic oil technique and its system | |
| CN110862841B (en) | Method for preparing natural gas from coal water slurry | |
| CN102320568A (en) | Method and device for preparing synthetic gas or hydrogen with BGL pressuring slag gasification and pure oxygen non-catalytic partial oxidation | |
| CN211311390U (en) | System for preparing synthesis gas by reforming and converting low-rank coal | |
| CN110655962A (en) | Method for converting coal into gas | |
| CN202208705U (en) | Device for preparing synthesis gas or hydrogen through BGL pressurizing molten slag gasification with pure oxygen non-catalytic partial oxidation | |
| CN110055106A (en) | A kind of method that low-order coal sub-prime prepares methanol and oil using Poly-generation | |
| CN103031154A (en) | Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier | |
| CN111253978A (en) | Method and system for preparing synthesis gas by using low-rank coal gas | |
| CN111253979A (en) | Method and system for preparing synthetic gas from coal | |
| CN111253975A (en) | Method for grading and utilizing low-rank coal | |
| CN111253974A (en) | Method and system for preparing synthesis gas by low-rank coal classification utilization | |
| CN201102901Y (en) | System for preparing synthetic gas or hydrogen gas from lurgi-furnace outlet coal gas by non-catalysis and partial oxidation | |
| CN109652129A (en) | A kind of method and system preparing synthesis gas using volatile matter in low-order coal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |