WO2013185594A1 - 适用于壳牌粉煤加压气化用煤的配煤方法 - Google Patents

适用于壳牌粉煤加压气化用煤的配煤方法 Download PDF

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WO2013185594A1
WO2013185594A1 PCT/CN2013/077081 CN2013077081W WO2013185594A1 WO 2013185594 A1 WO2013185594 A1 WO 2013185594A1 CN 2013077081 W CN2013077081 W CN 2013077081W WO 2013185594 A1 WO2013185594 A1 WO 2013185594A1
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Prior art keywords
coal
petroleum coke
ash
raw
gasification
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PCT/CN2013/077081
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English (en)
French (fr)
Inventor
何浩明
杨三可
郭丹
李华
黄世刚
陈忠阳
王波
杨锦成
李发中
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贵州天福化工有限责任公司
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Publication of WO2013185594A1 publication Critical patent/WO2013185594A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke

Definitions

  • the invention relates to a coal blending method, in particular to a coal blending method suitable for coal for pressurized gasification of Shell pulverized coal. Background technique
  • Shell pulverized coal gasification technology is the world's second-generation advanced coal gasification technology. It has the characteristics of wide adaptability of coal, large single series capacity, high gasification temperature, long operating cycle and good environmental benefits.
  • the main process of Shell pulverized coal gasification process is as follows: The raw coal is sent to the coal mill by the transportation facility after crushing, and the raw coal is ground into pulverized coal in the coal mill (90% particle size ⁇ 100 ⁇ ⁇ by mass) And drying, the coal powder is often pressed into the coal powder bin, the pressurized coal powder bin and the feed bin, and the coal powder is sent to the gasifier nozzle by high pressure nitrogen.
  • the oxygen from the air separation is pressurized by an oxygen compressor and preheated, mixed with the medium pressure superheated steam, and introduced into the nozzle.
  • the high-temperature gas at about 1500 °C at the top of the gasifier is cooled by the cold gas cooled by dust removal to about 900 °C and enters the waste heat boiler (SGC section).
  • the gas recovered by the waste boiler enters the dry dust removal (combined ceramic filter) and the wet scrubbing system, and the treated gas dust content is less than 1 mg / m 3 for subsequent steps.
  • the high-temperature slag produced by gasification in the gasification furnace is chilled from the chilling chamber flowing into the lower part of the gasification furnace, and the high-temperature slag is chilled to form a glass body of several metre meters, which can be used as building materials or for roadbed. .
  • Shell coal gasification has low requirements on coal activity, and the range of adaptation to coal ash melting point is wider than other gasification processes. It is also suitable for coal with high ash, high moisture and high sulfur content. However, high ash content coal will seriously reduce the economics of Shell coal gasification, which is reflected in two aspects. First, the higher the ash content in coal, the lower the effective gas production, the higher the oxygen consumption, and the lower the reaction volume of the gasifier. Economical, at the same time affect the effective gas production; Second, in order to adapt to high ash, slag conditions, equipment investment will increase. Under the same gasification reaction conditions, for every 1% increase in ash, oxygen consumption increases by 0.7% to 0.8%, and coal consumption increases by 1.3% to 1.5%.
  • Coal ash is an inert substance in coal, and its content and composition have little effect on the gasification reaction itself, but The amount of ash generated in the gasification process of coal with high ash content is bound to take away part of latent heat (carbon) and sensible heat, which reduces the thermal efficiency of coal. Moreover, the higher the ash content in the coal, the greater the transportation cost of the raw coal, the higher the gasification coal consumption and oxygen consumption, and the heavier the gasifier and ash treatment system load, which will affect the normal operation of the gasifier.
  • the optimum coal ash content of the process (shell) is 9% -19% (Xiang Aijuan, the influence of coal composition on the shell coal gasification process, “Fertilizer Industry”, Vol. 33, 2006) .
  • Guizhouzhouzhouzhouzhou is rich in coal resources and excellent in coal quality, but most of the coal is high ash coal.
  • coal ash in Guiyang is divided into 25%-35%.
  • the Liupanshui mining area is located in the southwestern part of Guizhouzhou province.
  • the coal mines in this area are large in number and complete in coal. Gas coal, fat coal, 1/3 coking coal, coking coal, lean coal, lean coal and anthracite are distributed.
  • Some coal mines have 3 coal seams.
  • the coal type, the coal seam is thin, the raw coal ash is high, generally between 20% and 40%, and the average value is 23.53%. Any of the above various coals or a single coal is higher than the design requirements of the Shell Pulverized Coal Gasification Process.
  • Petroleum coke is mainly used as a thinner to increase the blockiness of coke and improve the quality of coke.
  • Coke requires high carbon content in coal, low ash content, less harmful substances such as aluminum oxide and phosphorus pentoxide in ash, good coke reactivity, coke resistivity, especially high temperature resistivity, and volatile matter. Low, with appropriate strength and graininess of food, less water and stable, it has requirements for coal mainly from sulfur content, bond index, shrinkage and expansion.
  • the existing method to solve the high coal ash content of Shell pulverized coal pressurized gasification is mainly to use coal washing or clean coal to reduce the ash content of coal.
  • this method has higher cost and requires separate construction of coal washing workshop. Summary of the invention
  • the technical problem to be solved by the present invention is: to provide a low cost, simple coal blending method, which can effectively reduce raw coal ash, reduce slag discharge, and total ash, and is suitable for Shell.
  • the coal blending method of coal for pressurized coal gasification of pulverized coal can overcome the deficiencies of the prior art.
  • Coal blending method suitable for shell pulverized coal for pressurized gasification which method has higher ash content
  • the coal blending method comprises the following steps:
  • a. Detect the ash content of the raw coal, and calculate the required petroleum coke ratio according to the ash adjustment requirements; b. Put the raw coal and petroleum coke into the coal mill separately according to the calculation amount obtained in step a, and the raw coal after grinding by the coal mill 80% of the petroleum coke particles have a particle size between 5 ⁇ m and 90 ⁇ m;
  • the raw coal is coal
  • the petroleum coke is added 11.24-18.96%
  • the coal ash is divided into 23-28%
  • the petroleum coke is added 18.96-33.43%
  • the coal ash is divided into 28 -35%, adding petroleum coke 33.43-46.74%.
  • the coal used is a high ash coal having an ash content greater than 23%.
  • the petroleum coke used is ordinary petroleum coke, and the ash content is less than 1%.
  • the present invention uses petroleum coke produced in China or abroad, including spherical coke or sponge coke.
  • the coal has a dry basis moisture of from 0.1 to 5% (dry basis moisture).
  • the coal moisture content can be higher, and the moisture in the coal can be removed during the grinding drying phase.
  • the coal blending method comprises the following steps: using coal and petroleum coke as raw materials, wherein the coal blending ratio is 50-95%, and the petroleum coke blending ratio is 5-50%. It also added limestone, which accounts for 2-8% of the total mass of coal and petroleum coke (coking coal).
  • the ratio of coal and petroleum coke is used as a raw material, wherein the coal blending ratio is 85%, and the petroleum coke blending ratio is 15%.
  • Limestone accounts for 3-5% of total mass of coal and petroleum coke (coking coal).
  • the discharge rate of ground raw coal and petroleum coke is adjusted to the corresponding proportion.
  • the discharge rate of ground raw coal, petroleum coke and limestone is adjusted to grind 80% of the mixture particles to a particle size of 5 ⁇ m to 90 ⁇ m between.
  • the present invention utilizes Shell coal gasification to have low activity requirements on coal, and the adaptation range of coal ash melting point is wider than other gasification processes, and is also suitable for high ash and high sulfur content coals.
  • the advantage is that only the petroleum coke is used to adjust the inferior raw coal ash content of Guizhou within the design range, which can effectively utilize the inferior raw coal in Guizhou, and at the same time, the petroleum coke can effectively reduce the ash component of the inferior coal, so that it can be very good. Ensure that the effective gas volume of the Shell gasifier is increased and the total amount of ash is reduced.
  • Increasing the calorific value and fixed carbon content of the raw coal makes the economical efficiency of the unit gasifier's reaction volume increase, reduces the probability of clogging and failure of the waste heat recovery system, and reduces the probability of failure of the slag treatment system.
  • the invention adopts high ash coal and petroleum coke as raw materials for coal blending, because petroleum coke has calorific value, high fixed carbon, extremely low ash content, high sulfur content, and similar characteristics of volatile matter and coal volatile matter, so With the increase of petroleum coke ratio, the total ash content after coal blending will decrease, the calorific value and the fixed carbon will increase, which can overcome the shortcomings of high ash coal in the pressurized gasification process of Shell pulverized coal, effectively improve gas.
  • the production load of the furnace Compared with the use of clean coal for production, this blending coal is an economically viable measure, especially for local coal sources in Guizhou, through which many inferior coals can be effectively utilized.
  • the coal blending method can reduce the fine dust content in the crude gas while reducing the raw coal ash content, reduce the surface ash speed of the waste pot, and prolong the operation period of the device. Relatively use high-ash coal to produce synthetic ammonia, reduce the unit cost of synthetic ammonia by 300-500 yuan / ton, expand the range of purchase of shell pulverized coal pressurized gasification raw coal, so that coal resources can be rationally utilized.
  • Figure 1 shows the flow chart of Shell coal gasification process.
  • 1 is a gasifier
  • 2 is a slag removal system
  • 3 is a combination.
  • a gas cooler is a gas cooler.
  • Figure 2 shows the relationship between raw coal ash and effective gas production.
  • Figure 3 is a comparison of the cost of tons of ammonia under different unit prices. detailed description
  • the process flow is shown in Figure 1.
  • the raw coal is crushed, it is sent to the coal mill (Beijing Electric Power Equipment Factory, model: medium speed ZGM1237) by the transportation facility.
  • the raw coal is ground into coal powder in the coal mill (80% of the particle size is 5 by mass). -90 ⁇ ⁇ ) and dried, the pulverized coal is pressurized by pulverized coal (pressure 4.5 MPa), and the pulverized coal is sent to the gasification furnace 1 by high pressure nitrogen.
  • the oxygen from the air separation is pressurized by an oxygen compressor and preheated, mixed with the medium pressure superheated steam, and introduced into the gasification furnace 1.
  • Coal powder, oxygen and steam react in a temperature range of 1600 ° C in a gasifier 1 at a pressure of 3.8 MPa.
  • the high-temperature gas at about 1500 °C at the top of the gasifier is quenched by the dust-cooled cold gas to about 900 °C and enters the waste heat boiler.
  • the waste heat boiler is the syngas cooler 3 in Fig. 1, and the structure is that the syngas is taken in the furnace, the steam is taken in the furnace tube, the steam is heated by the syngas in stages, and the synthesis gas is cooled in stages.
  • the gas temperatures in the different sections of the SGC section are shown in Table 2 for the high ash raw coal.
  • the gas production capacity per ton of coal gasifier is 1606.84NM 3 /t standard coal, and the oxygen consumption per ton of standard coal is 657.28NM 3 /t standard coal.
  • the CO content of the effective gas component was 65% and H 2 was 16%.
  • the Tianfu coal gasification plant load can only be maintained below 85% (less than 85% of the oxygen load design standard), and the gas production is not Up to 85% of the design standard (gasification load).
  • the inlet of the slag removal system 2 has severe slag, and the temperature of the gasifier (1600 ° C is the highest value that the equipment can withstand) and other important process indicators are critical, and the equipment wear condition continues to deteriorate, and the waste ash accumulation speed Accelerate, the number of stops and maintenance of the device due to high ash increases, the system does not have high load, long cycle operation capability.
  • Figure 2 shows the gas production of coal with different ash at 80% load (oxygen load).
  • the design value of coal ash is 18.64%.
  • the coal sample is selected: Shanxi coal, which is analyzed to receive the base ash Aar, receive the base low calorific value Qnet, ar, receive the base fixed carbon FCar is 18.51%, 5977Kcal/Kg, and 66.88%, respectively.
  • Syngas production was carried out in accordance with the method of Comparative Example 1 without petroleum coke and limestone.
  • a chemical reaction occurs in a temperature range of 1600 ° C under a pressure of 3.8 MPa in a gasifier.
  • the oxygen load of the gasifier is 85%, and the operating load is increased within the normal operating range.
  • the pressure difference in the SGC section rises immediately, that is, the ash accumulation starts in the waste heat boiler, and the load cannot be 100%.
  • the actual processing load of the ash and slag system is 85-90%, and the gasifier temperature is 1590 °C.
  • the effective gas volume of the gasification furnace is 1660.61NM 3 /t standard coal, and the oxygen consumption per ton of standard coal is 659.55NM 3 /t standard coal.
  • the CO content of the effective gas component was 65% and H 2 was 17%.
  • the mixing ratio is 95%
  • the petroleum coke is Shandong Longkou petroleum coke (sponge rubber, the composition is shown in Table 1)
  • the compounding ratio is correspondingly 5%
  • the blending is uniform.
  • the coking coal after blending is received.
  • the base ash Aar, the received base low calorific value Qnet, ar, and the received base fixed carbon FCar were 21.08%, 6029Kcal/Kg, and 67.33%, respectively.
  • the ash melting point (FT ) of the coked coal is 1320 °C.
  • the effective gas volume of the gasification furnace is 1668.13NM 3 /t standard coal, and the oxygen consumption per ton of standard coal is 649.23NM 3 /t standard coal.
  • the CO component of the effective gas component was 66% and H 2 was 17%.
  • the coking coal after blending coal receives the base ash.
  • Aar, received base low calorific value Qnet, ar, received base fixed carbon FCar were 20.10%, 6159Kcal/Kg, 69.65%.
  • the ash melting point (FT) of the coking coal is 1375 °C.
  • the operation steps are the same as those in the first embodiment.
  • the effective gas volume of the gasification furnace is 1710.57NM 3 /t standard coal
  • the oxygen consumption per ton of standard coal is 643.25NM 3 /t standard coal.
  • the CO component of the effective gas component was 66% and H 2 was 18%.
  • the proportion of compounding is 84%
  • the petroleum coke is Shandong Yantai Longkou petroleum coke (the composition is shown in Table 1)
  • the mixing ratio is correspondingly 16%
  • the blending is uniform.
  • the coking coal after blending coal receives the base ash.
  • Aar, received base low calorific value Qnet, ar, received base fixed carbon FCar were 18.73%, 6228Kcal/Kg, 68.85%.
  • the ash melting point (FT) of the coked coal is 1352 °C.
  • the operation steps are the same as those in the first embodiment.
  • the effective gas volume of the gasification furnace is 1781.74NM 3 /t standard coal
  • the oxygen consumption per ton of standard coal is 638.43NM 3 /t standard coal.
  • the CO content of the effective gas component was 67% and H 2 was 18%.
  • the process of this embodiment can save about 160 T of raw coal per day.
  • the discharge of wastewater meets the design requirements, and the total amount of slag and ash is reduced by 150T.
  • the coal gasification unit can be stably operated at 100% full load, and the amount of syngas (CO+H 2 ) required to produce about 1570 tons of liquid ammonia capacity can be provided to the downstream unit every day.
  • the maximum load of only 85% the company can produce more than 500 tons of liquid ammonia per day.
  • the auxiliary equipment and downstream equipment capacity have been effectively utilized, and the operating costs have decreased accordingly.
  • the actual processing load of the ash and slag system is 95-100.%, and the gasifier temperature is 1550-1600.
  • the mixing ratio is 77%
  • the petroleum coke is Shandong Yantai Longkou petroleum coke (the composition is shown in Table 1)
  • the mixing ratio is correspondingly 23%
  • the blending is uniform.
  • the coking coal after blending receives the base ash.
  • Aar, received base low calorific value Qnet, ar, received base fixed carbon FCar were 17.22%, 6312Kcal/Kg, 70.33%.
  • the ash melting point (FT) of the coking coal was 1328 °C.
  • the operation steps are the same as those in the first embodiment.
  • the effective gas volume of the gas produced by the gasifier is 1821.29NM 3 /t standard coal, and the oxygen consumption per ton of standard coal is 633.65NM 3 /t standard coal.
  • the CO component of the effective gas component was 68% and H 2 was 19%.
  • the mixed coal can increase the effective gas volume of the ton of standard coal, reduce the oxygen consumption of the ton of standard coal, and change the CO and H 2 components of the effective gas component.
  • the shortcoming of low ash coal in the pressurized gasification process of Shell pulverized coal can be overcome, and the production load of the gasifier can be effectively improved.
  • the ash is divided into 21.08% of Guizhou high ash high ash melting temperature coal 200 tons, ash is 1% of Shandong Yantai Longkou petroleum coke 0 tons, respectively sent to two coal mills for grinding to 80% of the original coal
  • the diameter is between 5 ⁇ ⁇ and 90 ⁇ ⁇ .
  • Ash is divided into 22%, dry water moisture 1.91wt% Guizhou high ash high ash melting temperature coal 200 tons, ash is divided into 1% Shandong Yantai Longkou petroleum coke 9.163 tons, respectively sent to two coal mills for grinding to raw coal 80% of the particle size in petroleum coke is between 5 ⁇ m and 90 ⁇ m.
  • the ratio of the discharge rate of ground raw coal to petroleum coke is adjusted to 94:4, respectively, so that the raw coal powder and petroleum coke are uniformly mixed.
  • the coking coal after coal blending received a base ash of 21.02%, and the ash melting point (FT) of the coked coal was 1338 °C.
  • the coal gasification unit can be upgraded to full-load operation after driving, and the gas production reaches 142,000 square meters per hour of SHELL design.
  • the ash is divided into 28%, the dry water moisture is 2.41wt%, the Guizhou high ash high ash melting temperature coal is 200 tons, the ash is 0.98%, Shandong Yantai Longkou petroleum coke is 76 tons, which are sent to two coal mills for grinding to raw coal. 80% of the particle size in petroleum coke is between 5 ⁇ m and 90 ⁇ m.
  • the ratio of the discharge rate of ground raw coal to petroleum coke is adjusted to be 72.5:27.5, so that the raw coal powder and petroleum coke are uniformly mixed.
  • the coking coal after coal blending received a base ash of A. 20.9% and the coking coal had a ash melting point (FT) of 1,342 °C.
  • the coal gasification unit can be upgraded to full-load operation after driving, and the gas production reaches 142,000 square meters per hour of SHELL design.
  • the ash is divided into 25%, dry base moisture 2.97wt%, Guizhou high ash high ash melting temperature coal 200 tons, ash is 0.96% Shandong Yantai Longkou petroleum coke 60 tons, respectively sent to two coal mills for grinding to raw coal 80% of the particle size in petroleum coke is between 5 ⁇ m and 90 ⁇ m.
  • the coal gasification unit can be upgraded to full load after driving, and the gas production reaches 142,000 square meters per hour designed by SHELL.
  • Example 10
  • the ash is divided into 35%, dry water moisture 3.06wt% Guizhou high ash high ash melting temperature coal 200 tons, ash aliquot 1% Shandong Yantai Longkou petroleum coke 186 tons, respectively sent to two coal mills for grinding to raw coal 80% of the particle size in petroleum coke is between 5 ⁇ m and 90 ⁇ m.
  • the ratio of the discharge rate of ground raw coal to petroleum coke is adjusted to be 52:48, so that the raw coal powder and petroleum coke are uniformly mixed.
  • the coking coal after coal blending received a base ash Aer of 20.92%, and the coking coal had a ash melting point (FT) of 1340 °C.
  • the coal gasification unit can be upgraded to full-load operation after driving, and the gas production reaches 142,000 square meters per hour of SHELL design.
  • the ash is divided into 40%, dry water moisture 3.01wt% Guizhou high ash high ash melting temperature coal 200 tons, ash is 0.72% Shandong Yantai Longkou petroleum coke 100 tons, respectively sent to two coal mills for grinding to raw coal 80% of the particle size in petroleum coke is between 5 ⁇ m and 90 ⁇ m.
  • the discharge rate of ground raw coal and petroleum coke is adjusted separately to 66:33, so that the raw coal powder and petroleum coke are uniformly mixed.
  • the coking coal after coal blending received a base ash of A, 20.13%, and the coking coal had a ash melting point (FT) of 1,340 °C.
  • the coal gasification unit can be upgraded to full-load operation after driving, and the gas production reaches 142,000 square meters per hour of SHELL design.
  • Limestone, coal, and coke are sent to the coal mill through a conveying device with a conveying speed ratio of 2.9:32:65, and ground to a particle size of 10-90 ⁇ m, which accounts for 70% (the particle size distribution is determined by a laser particle size analyzer). Evenly, the coking coal after the analysis of coal blending received the low-level calorific value of Qnet, ar, and the received fixed carbon FCar were 6029Kcal/Kg and 67.33%, respectively.
  • the ash melting point (FT) of the coked coal (coal + petroleum coke + limestone) is 1368 °C. Table 3 High ash (ash 35%) Analysis of Guizhou coal ash components
  • the raw coal is sent to the coal mill by the transportation facility after crushing.
  • the raw coal is ground into pulverized coal (80% particle size 5-90 ⁇ by mass) in the coal mill and dried, and the coal powder is pressurized by pulverized coal. (Pressure 4.5 MPa), the pulverized coal was sent to the gasification furnace 1 by high pressure nitrogen.
  • the oxygen from the air separation is pressurized by an oxygen compressor and preheated, mixed with the medium pressure superheated steam, and introduced into the gasification furnace 1.
  • Coal powder, oxygen and steam react in a gasifier at a pressure of 4.0 MPa and a temperature range of 1500-1580 °C.
  • the high-temperature gas at about 1450 ° C at the top of the gasifier is quenched by the dust-cooled cold gas to about 800 ° C to enter the waste heat boiler.
  • the coal gasification unit can be upgraded to full load after driving.
  • the inlet of the slag removal system has no slag blocking, indicating that the slag has better fluidity than the coal blending method without limestone.
  • the gas production reached 142,000 square meters per hour designed by SHELL.
  • the effective gas volume of the gas produced by the gasifier is 1768.18NM 3 /t standard coal, and the oxygen consumption per ton of standard coal is 631.14NM 3 /t standard coal.
  • the CO content of the effective gas component was 66%, and the 3 ⁇ 4 was 17%.
  • the coke coal after analysis of coal blending received low-level calorific value Qnet, ar, and the base fixed carbon FCar were 6029Kcal/Kg and 67.33%, respectively.
  • the ash melting point (FT) of coking coal is 13:43 °C.
  • the pressure in the gasifier is 4.0MPa and the temperature is 1500-1550 °C.
  • the other steps are the same as in the embodiment 12.
  • the coal gasification unit can be upgraded to full load after driving, and the inlet of the slag removal system has no slag blocking.
  • the effective gas volume of the gasifier is 1756.13 NM 3 /t standard coal.
  • the oxygen consumption per ton of standard coal is 636.21 NM 3 /t standard coal.
  • the CO component of the effective gas component was 67% and H 2 was 18%.
  • Example 14 Take high-ash ash coal (ash 35%) dry base moisture 2.91wt%, compounding ratio 53.26%, petroleum coke is the Canadian imported spherical coke distributed by Rizhao Port (components are shown in Table 1, spherical coke), the proportion of compounding is 46.74 %, the ash component in the coal is analyzed, and the limestone is calculated according to the phase diagram of the ash melting point, and the ratio of limestone to the total mass of coal and coke is 3.0%.
  • Limestone, coal and coke are fed into the coal mill through a conveying device with a conveying speed ratio of 2.9:24:63, and ground to a particle size of 10-90 ⁇ m, which accounts for 70% (particle size distribution by laser particle size analyzer).
  • the coke coal after analysis of coal blending received low-level calorific value Qnet, ar, and received base fixed carbon FCar were 6029Kcal/Kg and 67.33%, respectively.
  • the ash melting point (FT) of coking coal (coal + petroleum coke + limestone) is 1345 °C.
  • the pressure in the gasifier is 4.0MPa and the temperature is 1500-1580 °C.
  • the other steps are the same as in the embodiment 12.
  • the coal gasification unit can be upgraded to full load after driving, and the inlet of the slag removal system has no slag blocking.
  • the effective gas volume of the gasification furnace is 1769.74 NM 3 /t standard coal.
  • the oxygen consumption per ton of standard coal is 631.96 NM 3 /t standard coal.
  • the CO component of the effective gas component was 66% and H 2 was 17%.
  • the coking coal after analysis of coal blending received the base ash Aar, the received base low calorific value Qnet, ar, and the received base fixed carbon FCar were 28%, 6029Kcal/Kg, and 67.33%, respectively.
  • the ash melting point (FT) of coking coal is 1328 °C.
  • the pressure in the gasifier is 4.0MPa and the temperature is 1500-1550 °C.
  • the other steps are the same as in the embodiment 12.
  • the coal gasification unit can be upgraded to full-load operation after driving.
  • the inlet of the slag removal system has no slag blocking.
  • the effective gas volume of the gasification furnace is 1768.23 NM 3 /t standard coal.
  • the oxygen consumption per ton of standard coal is 639.21NM 3 /t standard coal.
  • the CO component of the effective gas component was 66% and H 2 was 17%.
  • the compound coal can increase the effective gas volume of the shell coal gasification tons of standard coal, reduce the oxygen consumption per ton of standard coal, and change the CO and H 2 components of the effective gas components to make it more beneficial to the utilization of the ammonia alcohol cogeneration unit. At the same time, reduce the load of the ash and slag treatment equipment of the Shell Powder Coal Gasification Unit.
  • the method has effective practical significance for the high-ash inferior coal in Guizhou area, and has significant practical significance for the stable, high-efficiency and economic operation of pressurized coal gasification.
  • the method is applicable to the coal requirement of the pulverized coal pressurized gasification liquid slagging furnace, and has industrial applicability.

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Abstract

一种适用于壳牌粉煤加压气化用煤的配煤方法，该方法是将灰分高于21.08%的煤与石油焦进行混合，其煤与石油焦的用量要求为均匀混合后混合物中的灰分低于21.08%。该混配煤能提高壳牌粉煤气化吨标煤有效产气量，降低吨标煤耗氧量，并改变有效气组分中CO、H2组分使其更有利于氨醇联产装置的利用，同时降低壳牌粉煤气化装置灰、渣处理装置负荷。

Description

适用于壳牌粉煤加压气化用煤的配煤方法 技术领域
本发明涉及一种配煤方法， 具体涉及一种适用于壳牌粉煤加压气化用煤 的配煤方法。 背景技术
壳牌粉煤加压气化技术是目前世界上先进的第二代煤气化技术， 具有煤 种适应性广、 单系列能力大、 气化温度高、 运转周期长、 环境效益好等显著 特点。
壳牌粉煤加压气化工艺主要流程为： 原料煤经破碎由运输设施送至磨煤 机， 在磨煤机内将原料煤磨成煤粉 (按质量计， 其中 90 %粒度 <100 μ ιη)并干 燥， 煤粉经常压煤粉仓、 加压煤粉仓及给料仓， 由高压氮气将煤粉送至气化 炉喷嘴。 来自空分的氧气经氧压机加压并预热后与中压过热蒸汽混合后导入 喷嘴。 煤粉、 氧气及蒸汽在气化炉内 3.5-4.0MPa压力下， 1400-1600°C的温 度范围内发生化学反应， 碳转化率高达 99%以上， 气化产物为以 H2, CO为 主的合成气（达到 90%左右）。 气化炉顶部约 1500°C的高温煤气由除尘冷却 后的冷煤气激冷至 900°C左右进入废热锅炉 （SGC段） 。 经废锅回收热量后 的煤气进入干式除尘 （组合式陶瓷过滤器）及湿法洗涤系统， 处理后的煤气 尘含量小于 l mg / m3送后续工序。 在气化炉内气化产生的高温熔渣， 自流 入气化炉下部的激冷室进行激冷， 高温熔渣经激冷后形成数亳米大小的玻璃 体， 可作建筑材料或用于路基。
壳牌煤气化对煤的活性要求不高， 对煤的灰熔点适应范围比其它气化工 艺更宽， 对于高灰分、 高水份、 含硫量高的煤种也同样适应。 但是高灰分含 量煤种将严重降低壳牌煤气化经济性， 这体现在两个方面,一是煤中灰分越 高， 有效产气量就越低， 氧耗越高， 降低气化炉单位反应容积的经济性， 同 时影响有效气产量； 二是为适应高灰、 渣工况， 设备投资会增加。 在同样的 气化反应条件下，灰分每增加 1%,氧耗增加 0.7% ~ 0.8% ,煤耗增大 1.3% ~ 1.5%。 煤灰是煤中的惰性物质， 其含量和组成对气化反应本身影响不大， 但 灰分高的煤在气化过程中产生的灰渣量增加， 势必带走部分潜热 (碳)和显热， 使煤的热效率降低。 且煤中灰分含量越高， 原煤运输成本越大， 气化煤耗、 氧耗越高， 气化炉和灰渣处理系统负荷越重， 严重时会影响气化炉的正常运 行。 根据荷兰 DEMKOLEC电厂实际运行经验， 该工艺 （shell )最优化的煤 灰含量为 9 % -19 % (项爱娟，煤成分对 shell煤气化工艺的影响， 《化肥工业》 2006年第 33卷） 。
如果在实际生产中入炉煤煤质指标（灰分含量） 高于工艺设计煤样， 则 会导致系统始终处于设备运行的不稳定的极限工况， 合成气产量下降， 废锅 产汽下降， 排渣除灰超负荷 （堵渣堵灰）和灰水预处理系统不稳定引发停车 故障。 由于这类事故占壳牌总结的已开车装置内部事故的 40%之多， 已经引 起业内重视， 所以必须严格控制入炉煤的灰分在设计范围之内。
贵州省煤炭资源丰富， 煤质优良， 但大部分煤是高灰分煤， 如贵阳地区 煤灰分为 25%-35%。 六盘水矿区位于贵州省西南部， 该区煤矿数量较多， 煤 类齐全， 气煤、 肥煤、 1/3 焦煤、 焦煤、 瘦煤、 贫煤、 无烟煤均有分布， 有 些矿井一个煤层就有 3个煤种，煤层薄，原煤灰分高，一般在 20%-40%之间， 平均值为 23.53%。以上各种煤中的任两种煤或单独使用一种煤都高于壳牌粉 煤加压气化工艺的设计要求。
在原煤中配石油焦在其它领域已有使用， 如炼焦行业中高灰分煤添加石 油焦， 其中石油焦主要做为一种瘦化剂， 用于提高焦炭的块度， 改善焦炭的 质量。 焦炭要求煤固定碳含量高， 灰份低， 灰中有害物质三氧化二铝和五氧 化二磷等的含量要少， 焦炭反应性好， 焦炭电阻率特别是高温电阻率要大， 挥发份要低， 有适当的强度和食粮的块度， 水分少而稳定， 其对煤炭主要从 硫含量、 黏结指数、 收缩度和膨胀度等方面有要求。
现有解决壳牌粉煤加压气化原煤灰分高的办法主要是利用洗煤或精煤来 降低煤的灰分， 但这种方法成本较高、 需另行建造洗煤车间。 发明内容
针对现有技术的不足之处， 本发明要解决的技术问题是： 提供一种成本 低、 配煤方法简单， 可有效降低原煤灰分、 减少排渣、 灰总量的适用于壳牌 粉煤加压气化用煤的配煤方法， 可以克服现有技术的不足。
本发明目的通过下述技术方案来实现：
一种适用于壳牌粉煤加压气化用煤的配煤方法， 该方法是将灰分高于
21.08%的煤与石油焦进行混合， 其煤与石油焦的用量要求为均匀混合后混合 物中的灰分低于 21.08%。
所述的配煤方法包括如下步骤：
a、 检测原煤的灰分含量， 并根据灰分调节要求计算出所需石油焦比例； b、 根据 a步骤所得的计算量将原煤和石油焦分别投入磨煤机， 经磨煤机 研磨后的原煤和石油焦颗粒 80 %的粒径处于 5 μ m至 90 μ m之间；
c、 根据原煤与石油焦的用量， 分别调节研磨原煤与石油焦的出料速度， 使原煤粉末与石油焦粉末均匀混合。
其中，所述原煤即煤，当煤中灰分为 21.08-23% ,加入石油焦 11.24-18.96%; 当煤中灰分为 23-28% , 加入石油焦 18.96-33.43%; 当煤中灰分为 28-35%, 加 入石油焦 33.43-46.74%。
优选地， 所用煤为灰分高于 23%的高灰分煤。
其中， 所用的石油焦为普通石油焦， 灰分小于 1%。 本发明使用石油焦 为中国国内或国外所生产， 包括球状焦或海绵焦。
其中所述煤的干基水分为 0.1-5% (干基水分）。 煤含水分可以较高， 在磨 煤干燥阶段可以去除煤中的水分。
所述的配煤方法为： 以煤和石油焦为原料进行配比， 其中煤的配入比例 为 50-95% , 石油焦的配入比例为 5-50%。 还加入占煤和石油焦 （混焦煤） 总 质量比例 2-8%的石灰石。
优选地， 以煤和石油焦为原料进行配比， 其中煤的配入比例为 85% , 石 油焦的配入比例为 15%。 石灰石占煤和石油焦 （混焦煤） 总质量比例 3-5%。
其中磨煤时对原煤添加 2-8%的石灰石以调整灰熔点， 入炉煤灰熔点为 1350-1400°C。 所用煤为灰分高于 28%的高灰分煤。
其中， 根据原煤与石油焦的用量比例， 分别调节研磨原煤与石油焦的出 料速度为相应比例。 或者： 根据原煤与石油焦的用量比例， 分别调节研磨原煤与石油焦、 石 灰石的出料速度为相应比例， 加入磨煤机中研磨至混合物颗粒 80 %的粒径处 于 5 μ ιη至 90 μ ιη之间。
本发明的有益效果在于：
与现有技术比较， 本发明利用壳牌煤气化对煤的活性要求不高， 对煤的 灰熔点适应范围比其它气化工艺更宽， 对于高灰分、 含硫量高的煤种也同样 适应的优点， 只釆用石油焦将贵州劣质原煤灰分含量调整在设计范围内， 既 可使贵州劣质原煤得到有效利用， 同时因石油焦有效的降低了劣质煤的灰组 分， 这样就能很好的保证壳牌气化炉的有效气量提高， 灰渣总量减少。 提高 原料煤的热值和固定碳含量， 使得单位气化炉反应容积的经济性提升， 降低 废热回收系统出现堵塞故障停车的几率， 降低渣灰处理系统故障停车几率。
本发明以高灰分煤和石油焦为原料进行配煤， 因石油焦具有热值、 固定 碳很高， 灰分含量极低， 硫含量很高， 挥发分与煤挥发分相近的特性， 所以 随着石油焦配比的增加， 配煤后的总灰分会降低、 热值和固定碳会升高， 这 样可以克服高灰分煤在壳牌粉煤加压气化工艺中经济性低的缺点， 有效提高 气化炉的生产负荷。 与使用精煤进行生产相比， 本配煤是经济的可行措施， 尤其是针对贵州的当地煤源， 通过该配煤方案可以使许多劣质煤得到有效利 用。
本配煤方法在降低原煤灰分的同时还能降低粗煤气中的细粉尘含量， 降 低废锅表面积灰速度， 延长装置运行周期。 相对釆用高灰分煤生产合成氨， 降低合成氨单位成本 300-500元 /吨， 扩大壳牌粉煤加压气化原料煤釆购范围， 从而使煤炭资源得到合理利用。
本发明添加的石油焦， 主要侧重于改变粉煤在壳牌煤气化中燃烧效果， 对石油焦的含硫量、 挥发份以及刚性没有要求， 且最终产品为合成气而非固 定碳。 该混配煤能提高吨标煤产有效气量， 降低吨标煤耗氧量， 并改变有效 气组分中 CO、 H2组分。
附图说明
图 1 为壳牌煤气化工艺流程图。 图中 1为气化炉， 2为除渣系统， 3为合 成气冷却器。
图 2 为原煤灰分与有效气产量关系图。
图 3为不同原料单价下吨氨成本比较图。 具体实施方式
以下实施例用于说明本发明， 但不用来限制本发明的范围。
表 1为选取的煤样、 石油焦工业分析数值。 本发明相关数据计算方式按照 国标 GB/T212-2008、 GB/T211-2007以及 GB/T212-2008的规定计算。 贵州原混 煤的灰熔点 （FT )为 1322°C。
表 1 : 煤和石油焦成分
Figure imgf000007_0001
对比例 1
现有高灰分贵州煤（原混煤）， 经分析其收到基灰分 Aar、 收到基低位发 热量 Qnet,ar、 收到基固定碳 FCar分别为 22.16%、 5905Kcal/Kg、 65.46% (表 1 )。
工艺流程见图 1。 原料煤经破碎后由运输设施送至磨煤机（北京电力设备 总厂， 型号： 中速 ZGM1237 ), 在磨煤机内将原料煤磨成煤粉 (按质量计， 其 中 80 %粒度为 5-90 μ ιη)并干燥， 煤粉经粉煤加压（压力 4.5MPa ), 由高压氮气 将煤粉送至气化炉 1。来自空分的氧气经氧压机加压并预热后与中压过热蒸汽 混合后导入气化炉 1。 煤粉、 氧气及蒸汽在气化炉 1内 3.8MPa压力下， 1600°C 的温度范围内发生化学反应。 气化炉顶部约 1500°C的高温煤气由除尘冷却后 的冷煤气急冷至 900°C左右进入废热锅炉。 所述废热锅炉为图 1中合成气冷却 器 3, 其结构是炉膛内走合成气、 炉管内走蒸汽， 蒸汽被合成气分段升温， 合 成气则被分段冷却。 在 SGC段不同段的煤气温度见表 2之高灰分原煤。
气化炉吨标煤产有效气量为 1606.84NM3/t标煤， 吨标煤耗氧量为 657.28NM3/t标煤。 有效气组分中 CO为 65% , H2为 16%。
从 2010年 11月投料试车至 2012年 5月， 由于受高灰分原料煤的影响， 天福 煤气化装置负荷仅能维持在 85%以下（氧负荷设计标准的 85%以下）运行， 而 产气量不到设计标准 （气化负荷） 的 85%。 除渣系统 2的入口有严重的堵渣， 气化炉温度 （ 1600°C是设备可承受的最高值） 等重要工艺指标操控窗口已是 临界， 同时设备磨蚀情况持续恶化、 废锅积灰速度加快， 装置因高灰分停车 检修次数增加， 系统不具备高负荷、 长周期运行能力。 图 2为 80%负荷（氧负 荷） 下不同灰分的煤的产气量比较。
对比例 2:
按照壳牌粉煤加压气化工艺提出煤的灰分的设计值 18.64% , 挑选煤样： 山西煤， 经分析其收到基灰分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 18.51%、 5977Kcal/Kg、 66.88%。 不掺石油焦和石灰石， 按照对比 例 1的方法进行合成气生产。
气化炉内 3.8MPa压力下， 1600°C的温度范围内发生化学反应。
这时气化炉氧负荷为 85% , 正常运行操作范围内尝试提高运行负荷， 结 果 SGC段压差立即上升， 即废热锅炉内开始出现积灰现象， 无法将负荷达到 100%。 灰、 渣系统实际处理负荷 85-90%、 气化炉温度 1590°C。
气化炉吨标煤产有效气量为 1660.61NM3/t标煤， 吨标煤耗氧量为 659.55NM3/t标煤。 有效气组分中 CO为 65% , H2为 17%。
实施例 1
取高灰分贵州煤， 混配比例 95% , 石油焦为山东龙口石油焦 （海绵胶， 成分如表 1 ), 混配比例相应为 5% , 配合均匀， 经分析配煤后的混焦煤收到基 灰分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 21.08%、 6029Kcal/Kg、 67.33%。 混焦煤的灰熔点 （FT )为 1320°C。
原料煤经破碎由运输设施送至磨煤机 （北京电力设备总厂， 型号： 中速 磨煤机 ZGM123QG ), 在磨煤机内将原料煤磨成煤粉 (按质量计， 其中 80 %粒 度 5-90 μ ιη)并干燥， 电子皮带秤给煤机 （北京电力设备总厂， 型号 DPG60 ) 输送煤粉经粉煤加压 （压力 4.5MPa ), 由高压氮气将煤粉送至气化炉 1。 来自 空分的氧气经氧压机加压并预热后与中压过热蒸汽混合后导入气化炉 1。 煤 粉、 氧气及蒸汽在气化炉内 4.0MPa压力下， 1500-1600°C的温度范围内发生化 学反应。 气化炉顶部约 1500°C的高温煤气由除尘冷却后的冷煤气急冷至 900 °C左右进入废热锅炉（图 1 )。 在 SGC段不同段的煤气温度见表 2之配焦煤。 表 2第一行的编号为各段编号。
表 2: SGC段温度数据比较
Figure imgf000009_0001
这时气化炉吨标煤产有效气量为 1668.13NM3/t标煤， 吨标煤耗氧量为 649.23NM3/t标煤。 有效气组分中 CO为 66% , H2为 17%。
实施例 2
取高灰分贵州煤， 混配比例 90% , 石油焦为山东烟台龙口石油焦 （成分 如表 1 ), 混配比例相应为 10% , 配合均匀， 经分析配煤后的混焦煤收到基灰 分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 20.10%、 6159Kcal/Kg、 69.65%。 混焦煤的灰熔点 ( FT )为 1375 °C。
操作步骤同实施例 1。 这时气化炉吨标煤产有效气量为 1710.57NM3/t标 煤， 吨标煤耗氧量为 643.25NM3/t标煤。 有效气组分中 CO为 66% , H2为 18%。 实施例 3
取高灰分贵州煤， 混配比例 84% , 石油焦为山东烟台龙口石油焦 （成分 如表 1 ), 混配比例相应为 16% , 配合均匀， 经分析配煤后的混焦煤收到基灰 分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 18.73%、 6228Kcal/Kg、 68.85%。 混焦煤的灰熔点（FT )为 1352°C。 操作步骤同实施例 1。 这时气化炉吨标煤产有效气量为 1781.74NM3/t标煤， 吨标煤耗氧量为 638.43NM3/t标煤。 有效气组分中 CO为 67% , H2为 18%。
本实施例的方法可每天节约约 160T原煤。 废水排放量符合设计要求， 渣、 灰总量减少 150T。
实施例 3配焦后， 煤气化装置能稳定在 100%满负荷运行状态， 每天可 为下游装置提供生产约 1570余吨液氨产能所需合成气量（CO+H2 )，较之前 最高只能开 85%的负荷而言， 现公司每天可以多生产 500多吨液氨， 辅助装 置、 下游装置产能得到了有效的发挥， 运行成本相应下降。 灰、 渣系统实际 处理负荷 95-100.%、 气化炉温度 1550-1600。
实施例 4
取高灰分贵州煤， 混配比例 77% , 石油焦为山东烟台龙口石油焦 （成分 如表 1 ), 混配比例相应为 23% , 配合均匀， 经分析配煤后的混焦煤收到基灰 分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 17.22%、 6312Kcal/Kg、 70.33%。 混焦煤的灰熔点（FT )为 1328°C。 操作步骤同实施例 1。 这时气化炉吨标煤产有效气量为 1821.29NM3/t标煤， 吨标煤耗氧量为 633.65NM3/t标煤。 有效气组分中 CO为 68% , H2为 19%。
实施例 5
取高灰分贵州煤， 混配比例 70%, 石油焦为山东烟台龙口石油焦 （成分 如表 1 ), 混配比例相应为 30% , 配合均匀， 经分析配煤后的混焦煤收到基灰 分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 15.73%、 6511Kcal/Kg、 71.81%。 其余步骤同实施例 1。 这时气化炉吨标煤产有效气量 为 1879.54NM3/t标煤，吨标煤耗氧量为 629.58NM3/t标煤。有效气组分中 CO 为 69% , H2为 20%。
通过上述实施例 1-5可以看出， 该混配煤能提高吨标煤产有效气量， 降 低吨标煤耗氧量， 并改变有效气组分中 CO、 H2组分。 可以克服高灰分煤在 壳牌粉煤加压气化工艺中经济性低的缺点， 有效提高气化炉的生产负荷。 图
3为实施例 1-5的配煤方法带来的成本的变化。 由图 3可知， 即使煤焦价格 相差很大， 掺入石油焦可以有效地控制成本（合成气用于生产合成氨， 图 3 中最上方曲线）， 煤焦价格接近时， 本配煤方法可以降低生产成本。 原煤掺混 石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气量达到 SHELL 设计的 14.2万标方每小时。
实施例 6:
取灰分为 21.08%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 1%的山 东烟台龙口石油焦 0吨，分别送入两台磨煤机中进行研磨至原煤中 80 %的粒 径处于 5 μ ιη至 90 μ ιη之间。
实施例 7:
取灰分为 22%、干基水分 1.91wt%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 1%的山东烟台龙口石油焦 9.163吨，分别送入两台磨煤机中进行研磨 至原煤与石油焦中 80 %的粒径处于 5 μ ιη至 90 μ ιη之间。
根据原煤与石油焦的用量比， 分别调节研磨原煤与石油焦的出料速度比 例为 94:4, 使原煤粉末与石油焦均匀混合。 经分析配煤后的混焦煤收到基灰 分 Aar为 21.02%、 混焦煤的灰熔点 （ FT ) 为 1338°C。
原煤掺混石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气 量达到 SHELL设计的 14.2万标方每小时。
实施例 8:
取灰分为 28%、干基水分 2.41wt%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 0.98%的山东烟台龙口石油焦 76吨，分别送入两台磨煤机中进行研磨 至原煤与石油焦中 80 %的粒径处于 5 μ ιη至 90 μ ιη之间。
根据原煤与石油焦的用量比， 分别调节研磨原煤与石油焦的出料速度比 例为 72.5:27.5, 使原煤粉末与石油焦均匀混合。 经分析配煤后的混焦煤收到 基灰分 Aar为 20.9%、 混焦煤的灰熔点 ( FT )为 1342°C。
原煤掺混石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气 量达到 SHELL设计的 14.2万标方每小时。
实施例 9:
取灰分为 25%、干基水分 2.97wt%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 0.96%的山东烟台龙口石油焦 60吨，分别送入两台磨煤机中进行研磨 至原煤与石油焦中 80 %的粒径处于 5 μ ιη至 90 μ ιη之间。
根据原煤与石油焦的用量比， 分别调节研磨原煤与石油焦的出料速度比 例为 77:23 , 使原煤粉末与石油焦均匀混合。 经分析配煤后的混焦煤收到基 灰分 Aar为 21.00%、 混焦煤的灰熔点 ( FT )为 1341 °C。
原煤掺混石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气 量达到 SHELL设计的 14.2万标方每小时。 实施例 10:
取灰分为 35%、干基水分 3.06wt%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 1%的山东烟台龙口石油焦 186吨， 分别送入两台磨煤机中进行研磨 至原煤与石油焦中 80 %的粒径处于 5 μ ιη至 90 μ ιη之间。
根据原煤与石油焦的用量比， 分别调节研磨原煤与石油焦的出料速度比 例为 52:48, 使原煤粉末与石油焦均匀混合。 经分析配煤后的混焦煤收到基 灰分 Aar为 20.92%、 混焦煤的灰熔点 ( FT )为 1340°C。
原煤掺混石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气 量达到 SHELL设计的 14.2万标方每小时。
实施例 11:
取灰分为 40%、干基水分 3.01wt%的贵州高灰分高灰熔融温度煤 200吨， 灰分为 0.72%的山东烟台龙口石油焦 100吨， 分别送入两台磨煤机中进行研 磨至原煤与石油焦中 80 %的粒径处于 5 μ ιη至 90 μ ιη之间。
根据原煤与石油焦的用量比， 分别调节研磨原煤与石油焦的出料速度 66:33 , 使原煤粉末与石油焦均匀混合。 经分析配煤后的混焦煤收到基灰分 Aar为 20.13%、 混焦煤的灰熔点 ( FT ) 为 1340°C。
原煤掺混石油焦后， 煤气化装置在开车后就能提升至满负荷运行， 产气 量达到 SHELL设计的 14.2万标方每小时。
实施例 12
取高灰分（灰分 35% )、 干基水分 2.31wt%贵州煤， 混配比例 33% , 石油 焦为日照港经销的加拿大进口海绵焦 （成分如表 1 , 日照石油焦）， 混配比例 相应为 67%, 分析煤中灰组分（表 3 )灰熔点 FT为 1450°C , 按照灰熔点相图计 算石灰石的添加量， 为石灰石占煤和焦总质量的比例为 3.0%。 石灰石、 煤、 焦通过输送速度比例 2.9: 32:65的输送设备送入磨煤机，研磨至颗粒粒度 10-90 μ ιη占 70% (激光粒度仪测定粒度分布）。 配合均匀， 经分析配煤后的混焦煤 收到收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 6029Kcal/Kg、 67.33%。 混焦煤 (煤 +石油焦 +石灰石） 的灰熔点 ( FT ) 为 1368°C。 表 3 高灰分 （灰分 35%) 贵州煤灰组分分析
Figure imgf000013_0001
原料煤经破碎由运输设施送至磨煤机， 在磨煤机内将原料煤磨成煤粉 (按 质量计， 其中 80 %粒度 5-90 μ ιη)并干燥， 煤粉经粉煤加压（压力 4.5MPa ), 由 高压氮气将煤粉送至气化炉 1。来自空分的氧气经氧压机加压并预热后与中压 过热蒸汽混合后导入气化炉 1。 煤粉、 氧气及蒸汽在气化炉内 4.0MPa压力下， 1500-1580°C的温度范围内发生化学反应。 气化炉顶部约 1450°C的高温煤气由 除尘冷却后的冷煤气急冷至 800°C左右进入废热锅炉。
原煤掺混石油焦、 石灰石后， 煤气化装置在开车后就能提升至满负荷运 行， 除渣系统的入口没有堵渣， 说明渣的流动性好于没有掺石灰石的配煤方 式。 产气量达到 SHELL设计的 14.2万标方每小时。 这时气化炉吨标煤产有 效气量为 1768.18NM3/t标煤， 吨标煤耗氧量为 631.14NM3/t标煤。 有效气组 分中 CO为 66%, ¾为 17%。
实施例 13
取高灰分（灰分 28% )、 干基水分 3.04wt%贵州煤， 混配比例 25% , 石油 焦为日照港经销的加拿大进口海绵焦 （成分如表 1 , 日照石油焦）， 混配比例 相应为 75%, 分析煤中灰组分， 石灰石添加量按照灰熔点相图计算， 石灰石 占煤和焦总质量的比例为 3.0%。 石灰石、 煤、 焦通过输送速度比例 2.9: 24: 63的输送设备送入磨煤机， 研磨至颗粒粒度 10-90 μ ιη占 70% (激光粒度仪测 粒度分布）。 配合均匀， 经分析配煤后的混焦煤收到基低位发热量 Qnet,ar、 收 到基固定碳 FCar分别为 6029Kcal/Kg、 67.33%。 焦煤（煤 +石油焦 +石灰石）的 灰熔点 ( FT )为 13:43°C。
气化炉内 4.0MPa压力， 1500-1550°C的温度。 其他步骤同实施例 12。
原煤掺混石油焦、 石灰石后， 煤气化装置在开车后就能提升至满负荷运 行， 除渣系统的入口没有堵渣， 气化炉吨标煤产有效气量为 1756.13NM3/t标 煤， 吨标煤耗氧量为 636.21NM3/t标煤。 有效气组分中 CO为 67%, H2为 18%。 实施例 14 取高灰分贵州煤（灰分 35% )干基水分 2.91wt%, 混配比例 53.26%, 石油 焦为日照港经销的加拿大进口球形焦 （成分如表 1 , 球形焦）， 混配比例相应 为 46.74%, 分析煤中灰组分， 石灰石按照灰熔点相图计算添加量， 石灰石占 煤和焦总质量的比例为 3.0%。 石灰石、 煤、 焦通过输送速度比例 2.9: 24: 63 的输送设备送入磨煤机， 研磨至颗粒粒度 10-90 μ ιη占 70% (激光粒度仪测粒 度分布）。 配合均匀， 经分析配煤后的混焦煤收到基低位发热量 Qnet,ar、 收到 基固定碳 FCar分别为 6029Kcal/Kg、 67.33%。 焦煤（煤 +石油焦 +石灰石）的灰 熔点 （FT ) 为 1345°C。
气化炉内 4.0MPa压力， 1500-1580°C的温度。 其他步骤同实施例 12。
原煤掺混石油焦、 石灰石后， 煤气化装置在开车后就能提升至满负荷运 行， 除渣系统的入口没有堵渣， 气化炉吨标煤产有效气量为 1769.74 NM3/t标 煤， 吨标煤耗氧量为 631.96NM3/t标煤。 有效气组分中 CO为 66%, H2为 17%。 实施例 15
取高灰分贵州煤（灰分 30% ), 干基水分 1.91wt%。 混配比例 60% , 石油 焦为日照港经销的加拿大进口海绵焦 （成分如表 1 , 日照石油焦）， 混配比例 相应为 40%, 分析煤中灰组分， 按照灰熔点相图计算石灰石添加量， 石灰石 占煤和焦总质量的比例为 3.0%。 石灰石、 煤、 石油焦混合后粒度 10-90 μ ιη占 80%。 配合均匀， 经分析配煤后的混焦煤收到基灰分 Aar、 收到基低位发热量 Qnet,ar、 收到基固定碳 FCar分别为 28%、 6029Kcal/Kg、 67.33%。 焦煤 （煤 + 石油焦 +石灰石） 的灰熔点 ( FT ) 为 1328°C。
气化炉内 4.0MPa压力， 1500-1550°C的温度。 其他步骤同实施例 12。
原煤掺混石油焦、 石灰石后， 煤气化装置在开车后就能提升至满负荷运 行， 除渣系统的入口没有堵渣， 气化炉吨标煤产有效气量为 1768.23NM3/t标 煤， 吨标煤耗氧量为 639.21NM3/t标煤。 有效气组分中 CO为 66%, H2为 17%。
其他粉煤加压气化技术如 GSP、 航天炉等， 对入炉煤的灰分、 灰熔点要 求和壳牌技术的工艺要求的原理一致， 当煤的灰分高时， 会导致负荷下降、 结渣、 经济性降低的后果。 因此本配煤方法同样适用于其他粉煤加压气化技 术。 以上的实施例仅仅是对本发明的优选实施方式进行描述，并非对本发明的 范围进行限定， 在不脱离本发明设计精神的前提下， 本领域普通工程技术人 员对本发明的技术方案作出的各种变型和改进， 均应落入本发明的权利要求 书确定的保护范围内。 工业实用性 本发明公开的用于壳牌粉煤加压气化用煤的配煤方法， 将灰分高于
21.08%的煤与石油焦进行混合， 均匀混合后混合物中的灰分低于 21.08%。该 混配煤能提高壳牌粉煤气化吨标煤产有效气量， 降低吨标煤耗氧量， 并改变 有效气组分中 CO、 H2组分使其更有利于氨醇联产装置的利用， 同时降低壳 牌粉煤气化装置灰、 渣处理装置负荷。 该方法对贵州地区高灰分劣质煤的有 效利用， 对于粉煤加压气化的稳定、 高效、 经济运行具有显著的现实意义， 对于实现粉煤加压气化原料多样化及煤炭资源的合理利用具有重要的社会效 益。 该方法适用于粉煤加压气化液态排渣炉的用煤要求， 具有工业实用性。

Claims

权 利 要 求 书
1、 一种适用于壳牌粉煤加压气化用煤的配煤方法， 其特征在于： 该方法 是将灰分高于 21.08%的煤与石油焦进行混合， 其煤与石油焦的用量要求为均 匀混合后混合物中的灰分低于 21.08%。
2、 根据权利要求 1所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 它包括如下步骤：
a、 检测原煤的灰分含量， 并根据灰分调节要求计算出所需石油焦比例； b、 根据 a步骤所得的计算量将原煤和石油焦分别投入磨煤机， 经磨煤机 研磨后的原煤和石油焦颗粒 80 %的粒径处于 5 μ m至 90 μ m之间；
c、 根据原煤与石油焦的用量， 分别调节研磨原煤与石油焦的出料速度， 使原煤粉末与石油焦粉末均匀混合。
3、 根据权利要求 1所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 所用煤为灰分高于 23%的高灰分煤。
4、 根据权利要求 1所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 所用的石油焦为普通石油焦， 灰分小于 1%。
5、 根据权利要求 1所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 所述煤的干基水分为 0.1-5%。
6、 根据权利要求 2所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 以煤和石油焦为原料进行配比， 其中煤的配入比例为 50-95% , 石 油焦的配入比例为 5-50% , 还加入占煤和石油焦总质量的 2-8%的石灰石。
7、 根据权利要求 6所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其 特征在于： 以煤和石油焦为原料进行配比， 其中煤的配入比例为 85% , 石油 焦的配入比例为 15%, 石灰石占煤和石油焦总质量的 3-5%。
8、 根据权利要求 1或 3所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其特征在于： 磨煤时对原煤添加 2-8%的石灰石以调整灰熔点， 入炉煤灰熔点 为 1350-1400°C。
9、 根据权利要求 1或 3所述的适用于壳牌粉煤加压气化用煤的配煤方法， 其特征在于： 根据原煤与石油焦的用量比例， 分别调节研磨原煤与石油焦的 出料速度为相应比例。
10、 根据权利要求 6-9任一所述的适用于壳牌粉煤加压气化用煤的配煤方 法， 其特征在于： 根据原煤与石油焦的用量比例， 分别调节研磨原煤与石油 焦、 石灰石的出料速度为相应比例， 加入磨煤机中研磨至混合物颗粒 80 %的 粒径处于 5 μ m至 90 μ m之间。
PCT/CN2013/077081 2012-06-13 2013-06-09 适用于壳牌粉煤加压气化用煤的配煤方法 WO2013185594A1 (zh)

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