CN102585913B - Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology - Google Patents
Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology Download PDFInfo
- Publication number
- CN102585913B CN102585913B CN2012100641393A CN201210064139A CN102585913B CN 102585913 B CN102585913 B CN 102585913B CN 2012100641393 A CN2012100641393 A CN 2012100641393A CN 201210064139 A CN201210064139 A CN 201210064139A CN 102585913 B CN102585913 B CN 102585913B
- Authority
- CN
- China
- Prior art keywords
- semi
- coke
- fluidized bed
- gas
- temperature
- 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
- 239000000571 coke Substances 0.000 title claims abstract description 162
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 111
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000005516 engineering process Methods 0.000 title claims abstract description 15
- 239000003034 coal gas Substances 0.000 title claims abstract description 6
- 239000007789 gas Substances 0.000 claims abstract description 55
- 238000010438 heat treatment Methods 0.000 claims abstract description 51
- 239000003245 coal Substances 0.000 claims abstract description 50
- 238000002485 combustion reaction Methods 0.000 claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000003546 flue gas Substances 0.000 claims abstract description 32
- 239000002918 waste heat Substances 0.000 claims abstract description 26
- 239000011269 tar Substances 0.000 claims abstract description 20
- 239000007787 solid Substances 0.000 claims abstract description 10
- 239000000428 dust Substances 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims description 30
- 239000002245 particle Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 6
- 239000011286 gas tar Substances 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 238000009826 distribution Methods 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 238000010304 firing Methods 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000010248 power generation Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 125000002950 monocyclic group Chemical group 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000002076 thermal analysis method Methods 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
本发明涉及一种基于流化床热解技术的煤气焦油半焦蒸汽多联产方法。该方法以高温半焦为热载体，煤与高温半焦在流化床热解炉中混合升温，析出挥发分，挥发分经冷却分离得到焦油和热解煤气，而半焦的一部分输出作半焦产品，另一部分则送至流化床半焦加热炉，与送入的少量空气发生燃烧反应，少量半焦燃烧后所释放的热量加热所送入的全部半焦，加热后的半焦随烟气进入旋风分离器，分离下来的高温半焦作为热载体送入流化床热解炉，而气固分离后的烟气则被送入补燃式余热锅炉，燃尽烟气中少量的可燃成分，生产蒸汽，然后进入空气预热器加热燃烧所需的空气，最后经除尘器除尘后排空。本发明的优点在于实现了煤的分级转化，提高了煤的利用效率和效益。
The invention relates to a method for cogeneration of coal gas tar and semi-coke steam based on fluidized bed pyrolysis technology. In this method, high-temperature semi-coke is used as the heat carrier. Coal and high-temperature semi-coke are mixed and heated in a fluidized bed pyrolysis furnace to precipitate volatile matter, which is cooled and separated to obtain tar and pyrolysis gas, and part of the semi-coke is output as semi-coke. coke products, and the other part is sent to the fluidized bed semi-coke heating furnace, where it reacts with a small amount of air fed in, and the heat released after the combustion of a small amount of semi-coke heats all the semi-coke fed in. The flue gas enters the cyclone separator, and the separated high-temperature semi-coke is sent to the fluidized bed pyrolysis furnace as a heat carrier, while the flue gas after gas-solid separation is sent to a supplementary combustion waste heat boiler to burn off a small amount of The combustible components produce steam, then enter the air preheater to heat the air required for combustion, and finally go through the dust collector and then evacuate. The invention has the advantages of realizing the graded conversion of coal and improving the utilization efficiency and benefit of coal.
Description
技术领域 technical field
本发明涉及煤转化领域，特别是涉及一种基于流化床热解技术的煤气焦油半焦蒸汽多联产方法及装置。The invention relates to the field of coal conversion, in particular to a gas tar semi-coke steam polygeneration method and device based on fluidized bed pyrolysis technology.
背景技术 Background technique
我国能源资源的显著特征是富煤、少油、缺气。根据我国资源条件的特殊性，发展以煤热解为基础的煤气焦油半焦蒸汽多联产技术，用储量相对丰富的煤炭资源制取焦油和煤气来替代储量相对匮乏的油气资源以及生产各种化学品，同时伴产半焦和蒸汽，满足社会经济发展的需求，这不失为一种合理利用资源的好途径。另外，煤是由水分、挥发分、灰分及固定碳等多种物质构成的混合体，是复杂的碳氢高分子混合物。但目前煤炭资源往往被作为单一用途来利用，大部分以直接燃烧为主，其他气化、液化也是以单一过程为主。煤直接燃烧是单纯地把煤作为燃料利用，不能有效利用煤中所含的高价值组分；而在煤的气化、液化等单个转化过程中，由于固体颗粒反应速度随转化程度增加而减慢，要想取得较高的转化效率，必须采取措施转化较难转化的部分，这就导致技术复杂，设备庞大，投资及生产成本高。因此，发展以煤热解为基础的多联产技术，既能有效利用煤中的高价值组分，又能降低煤转化过程中的难度，提高煤的转化效率和利用效率，降低投资及生产成本，降低污染排放，实现煤炭资源利用的最优化。The salient features of my country's energy resources are rich in coal, low in oil and short of gas. According to the particularity of our country's resource conditions, develop coal gas, tar, semi-coke and steam polygeneration technology based on coal pyrolysis, use relatively abundant coal resources to produce tar and gas to replace relatively scarce oil and gas resources, and produce various Chemicals, together with semi-coke and steam, meet the needs of social and economic development, which is a good way to use resources rationally. In addition, coal is a mixture of moisture, volatile matter, ash, and fixed carbon, and is a complex mixture of hydrocarbons and polymers. But at present, coal resources are often used as a single purpose, most of which are mainly used for direct combustion, and other gasification and liquefaction are also mainly used for a single process. The direct combustion of coal simply uses coal as a fuel, and cannot effectively utilize the high-value components contained in coal; and in the single conversion process of coal gasification and liquefaction, the reaction speed of solid particles decreases with the increase of conversion degree. Slow, in order to obtain a higher conversion efficiency, measures must be taken to convert the part that is difficult to convert, which leads to complex technology, huge equipment, high investment and production costs. Therefore, the development of polygeneration technology based on coal pyrolysis can not only effectively utilize high-value components in coal, but also reduce the difficulty of coal conversion process, improve coal conversion efficiency and utilization efficiency, and reduce investment and production. cost, reduce pollution emissions, and optimize the utilization of coal resources.
煤热解具有工艺过程简单，加工条件温和，投资少，生产成本低等优势。煤热解工艺按加热方式可分为外热式和内热式两类。外热式煤热解工艺热效率低，煤料加热不均，半焦质量不匀，挥发产物的二次分解严重，设备复杂，投资大，产能小；内热式煤热解工艺克服了外热式的缺点，借助热载体把热量直接传递给煤料，受热后的煤发生热解反应产生煤气、焦油和半焦。内热式煤热解工艺根据供热介质不同，又分为气体热载体煤热解和固体热载体煤热解。气体热载体煤热解工艺多采用燃料燃烧所产生的高温烟气或者煤热解所产生的高温煤气作热载体。采用高温烟气作气体热载体，会导致煤热解析出的挥发产物被烟气稀释，从而使得煤气热值不高，有效组分浓度低，利用价值低；采用高温煤气作气体热载体，出炉热解煤气冷却后又有部分煤气再次通过外加热方式加热为高温煤气作热载体，耗能大，热效率低，且消耗掉较大部分的高品位产物煤气。固体热载体煤热解工艺则利用高温循环灰或高温半焦与煤在热解室内混合，利用固体热载体的显热将煤热解。采用高温循环灰作固体热载体，由于煤热解所产生的半焦中掺混了大量灰热载体，灰分含量高、热值低，半焦产品品质较低，除燃烧利用外用途受到限制；而采用高温半焦作固体热载体可以获得品质较高的半焦，易于半焦产品下一阶段的利用。Coal pyrolysis has the advantages of simple process, mild processing conditions, less investment, and low production cost. According to the heating method, the coal pyrolysis process can be divided into two types: external heat type and internal heat type. The external heating coal pyrolysis process has low thermal efficiency, uneven heating of coal materials, uneven semi-coke quality, serious secondary decomposition of volatile products, complex equipment, large investment, and small production capacity; the internal heating coal pyrolysis process overcomes the external heating The disadvantage is that the heat is directly transferred to the coal material by means of the heat carrier, and the heated coal undergoes pyrolysis reaction to produce gas, tar and semi-coke. The internal heat coal pyrolysis process is divided into gas heat carrier coal pyrolysis and solid heat carrier coal pyrolysis according to different heating media. Gas heat carrier Coal pyrolysis process mostly uses high-temperature flue gas produced by fuel combustion or high-temperature gas produced by coal pyrolysis as heat carrier. The use of high-temperature flue gas as the gas heat carrier will cause the volatile products released by coal thermal analysis to be diluted by the flue gas, so that the calorific value of the gas is not high, the concentration of effective components is low, and the use value is low; After the pyrolysis gas is cooled, part of the gas is heated again by external heating to high-temperature gas as a heat carrier, which consumes a lot of energy, has low thermal efficiency, and consumes a large part of the high-grade product gas. The solid heat carrier coal pyrolysis process uses high-temperature circulating ash or high-temperature semi-coke to mix with coal in the pyrolysis chamber, and uses the sensible heat of the solid heat carrier to pyrolyze the coal. High-temperature circulating ash is used as the solid heat carrier. Since the semi-coke produced by coal pyrolysis is mixed with a large amount of ash heat carrier, the ash content is high, the calorific value is low, the quality of the semi-coke product is low, and its use is limited except for combustion and utilization; Using high-temperature semi-coke as a solid heat carrier can obtain high-quality semi-coke, which is easy to use in the next stage of semi-coke products.
发明内容 Contents of the invention
本发明要解决的技术问题是，克服现有技术的不足，提供一种基于流化床热解技术的煤气焦油半焦蒸汽多联产方法。The technical problem to be solved by the present invention is to overcome the deficiencies of the prior art, and provide a gas tar semi-coke steam polygeneration method based on fluidized bed pyrolysis technology.
为解决技术问题，本发明的解决方案是：For solving technical problem, solution of the present invention is:
提供一种基于流化床热解技术的煤气焦油半焦蒸汽多联产方法，该方法基于流化床热解技术，以半焦为热载体，实现煤气、焦油、半焦和蒸汽联产；其内容具体包括：Provide a method for cogeneration of gas, tar, semi-coke and steam based on fluidized bed pyrolysis technology. The method is based on fluidized bed pyrolysis technology and uses semi-coke as a heat carrier to realize the co-production of gas, tar, semi-coke and steam; Its content specifically includes:
(1)将原料煤与半焦在流化床热解炉中混合，煤与半焦的混合比例为1∶5～1∶15，控制运行温度为500～800℃；原料煤发生热解并析出挥发分，挥发分经旋风分离器分离后进入煤气冷却系统，冷却分离得到焦油和热解煤气；热解煤气的一部分作为流化介质再循环回流化床热解炉，剩余热解煤气经净化后作为化工合成原料或燃气燃料，收集到的焦油用于后续加工利用，经旋风分离器分离下来的半焦颗粒经冷却后作为半焦产品；(1) Mix the raw coal and semi-coke in a fluidized bed pyrolysis furnace, the mixing ratio of coal and semi-coke is 1:5-1:15, and the operating temperature is controlled at 500-800°C; the raw coal is pyrolyzed and The volatile matter is separated by the cyclone separator and then enters the gas cooling system, and the tar and pyrolysis gas are obtained by cooling and separation; part of the pyrolysis gas is used as a fluidized medium to recirculate back to the fluidized bed pyrolysis furnace, and the remaining pyrolysis gas is passed through After purification, it is used as chemical synthesis raw material or gas fuel. The collected tar is used for subsequent processing and utilization. The semi-coke particles separated by the cyclone separator are cooled and used as semi-coke products;
(2)将流化床热解炉内的部分半焦排出并冷却后作为半焦产品，排出量控制在流化床热解炉给煤量的60％～90％，具体由流化床热解炉实际运行时的物料平衡来决定；另有一部分半焦则送至流化床半焦加热炉中，在半焦加热炉中使其中少部分半焦与空气发生燃烧反应，燃烧所放出的热量用于加热剩余未燃烧的那部分半焦颗粒以及烟气，控制流化床半焦加热炉运行温度为850～1000℃；加热后的高温半焦由高温烟气携带进入高温旋风分离器中进行气固分离，分离下来的高温半焦返送至流化床热解炉为煤热解提供热载体，而分离后的高温烟气进入补燃式余热锅炉；从流化床热解炉送入到半焦加热炉的半焦量，由最终通过半焦加热炉获得的高温半焦能将流化床热解炉加热到500～800℃来决定；(2) Discharge and cool part of the semi-coke in the fluidized bed pyrolysis furnace as a semi-coke product. It is determined by the material balance during the actual operation of the furnace; another part of the semi-coke is sent to the fluidized bed semi-coke heating furnace, and a small part of the semi-coke is burned with air in the semi-coke heating furnace. The heat is used to heat the remaining unburned semi-coke particles and flue gas, and the operating temperature of the fluidized bed semi-coke heating furnace is controlled at 850-1000°C; the heated high-temperature semi-coke is carried by the high-temperature flue gas into the high-temperature cyclone separator Gas-solid separation is carried out, and the separated high-temperature semi-coke is sent back to the fluidized bed pyrolysis furnace to provide heat carrier for coal pyrolysis, and the separated high-temperature flue gas enters the afterburning waste heat boiler; it is sent from the fluidized bed pyrolysis furnace The amount of semi-coke to the semi-coke heating furnace is determined by the high-temperature semi-coke obtained through the semi-coke heating furnace that can heat the fluidized bed pyrolysis furnace to 500-800 °C;
(3)分离后的高温烟气携带有可燃气体和少量细半焦颗粒，全部进入补燃式余热锅炉，在这里使这些可燃组分进一步燃尽，所产生的高温烟气通过换热将水加热为蒸汽；经换热后的高温烟气进入空气预热器加热空气，加热后的空气分别送入流化床半焦加热炉和补燃式余热锅炉提供燃烧所需氧气；通过空气预热器换热后的烟气经除尘后排空。(3) The separated high-temperature flue gas carries combustible gas and a small amount of fine semi-coke particles, all of which enter the post-combustion waste heat boiler, where these combustible components are further burnt out, and the high-temperature flue gas generated heats the water Heating is steam; the high-temperature flue gas after heat exchange enters the air preheater to heat the air, and the heated air is respectively sent to the fluidized bed semi-coke heating furnace and the supplementary combustion waste heat boiler to provide the oxygen required for combustion; through air preheating After heat exchange, the flue gas is evacuated after dust removal.
本发明中，所述对半焦进行冷却是采用室温下的水作冷却剂在半焦冷却装置中实现换热的，被加热后的冷却水被送入补燃式余热锅炉中进一步用于生产蒸汽产品。In the present invention, the semi-coke is cooled by using water at room temperature as a coolant to realize heat exchange in the semi-coke cooling device, and the heated cooling water is sent into a supplementary combustion waste heat boiler for further production steam products.
进一步地，本发明还提供了一种用于实现前述方法的基于流化床热解技术的煤气焦油半焦蒸汽多联产装置，包括流化床热解炉和流化床半焦加热炉；流化床热解炉侧面下部设有给料口，流化床热解炉的顶部出口通过管路依次接一级旋风分离器和二级旋风分离器，二级旋风分离器的出口接至煤气冷却系统，两个旋风分离器的底部通过管路接至半焦冷却装置；煤气冷却系统设焦油排出口和热解煤气排出口，热解煤气排出口通过管路同时接至煤气对外输出口和位于流化床热解炉底部的再循环热解煤气的入口；流化床热解炉底部还设有炉底半焦排出装置，通过管路与半焦冷却装置相连接，半焦冷却装置设半焦产品出口；流化床热解炉一侧的出料口处设有高温机械阀，高温机械阀通过管路与第一返料器相连，第一返料器接至位于流化床半焦加热炉底部的半焦入口；流化床半焦加热炉顶部出口依次连接一级高温旋风分离器和二级高温旋风分离器，两个高温旋风分离器的底部均接至第二返料器，第二返料器接至流化床热解炉下部的高温半焦入口；二级高温旋风分离器的顶部通过管路接至补燃式余热锅炉，补燃式余热锅炉的气体出口依次接空气预热器和除尘器，除尘器设烟气出口；空气预热器的热空气出口侧分别接至流化床半焦加热炉底部的空气入口和补燃式余热锅炉的空气入口。Further, the present invention also provides a gas tar semi-coke steam polygeneration device based on fluidized bed pyrolysis technology for realizing the aforementioned method, including a fluidized bed pyrolysis furnace and a fluidized bed semi-coke heating furnace; The lower part of the side of the fluidized bed pyrolysis furnace is provided with a feed port, and the top outlet of the fluidized bed pyrolysis furnace is connected to the first-level cyclone separator and the second-level cyclone separator in turn through the pipeline, and the outlet of the second-level cyclone separator is connected to the gas Cooling system, the bottoms of the two cyclone separators are connected to the semi-coke cooling device through pipelines; the gas cooling system is provided with a tar discharge port and a pyrolysis gas discharge port, and the pyrolysis gas discharge port is connected to the external gas output port and the The inlet of recirculating pyrolysis gas is located at the bottom of the fluidized bed pyrolysis furnace; the bottom of the fluidized bed pyrolysis furnace is also equipped with a semi-coke discharge device at the bottom of the furnace, which is connected to the semi-coke cooling device through pipelines, and the semi-coke cooling device is set Semi-coke product outlet; there is a high-temperature mechanical valve at the discharge port on one side of the fluidized bed pyrolysis furnace. The semi-coke inlet at the bottom of the coke heating furnace; the top outlet of the fluidized bed semi-coke heating furnace is connected to the first-level high-temperature cyclone separator and the second-level high-temperature cyclone separator in turn, and the bottoms of the two high-temperature cyclone separators are connected to the second feeder , the second feeder is connected to the high-temperature semi-coke inlet at the lower part of the fluidized bed pyrolysis furnace; the top of the secondary high-temperature cyclone separator is connected to the post-combustion waste heat boiler through a pipeline, and the gas outlet of the post-combustion waste heat boiler is connected to the Air preheater and dust remover, the dust remover is equipped with a flue gas outlet; the hot air outlet side of the air preheater is respectively connected to the air inlet at the bottom of the fluidized bed semi-coke heating furnace and the air inlet of the post-combustion waste heat boiler.
本发明中，流化床热解炉一侧的出料口处所设的高温机械阀，布置于流化床热解炉的布风板以上1～4米的位置。In the present invention, the high-temperature mechanical valve provided at the discharge port on one side of the fluidized bed pyrolysis furnace is arranged at a position 1 to 4 meters above the air distribution plate of the fluidized bed pyrolysis furnace.
本发明中，所述半焦冷却装置的换热器使用室温下的水作为冷却剂，其冷却水出口通过管路连接至补燃式余热锅炉的供水入口。In the present invention, the heat exchanger of the semi-coke cooling device uses water at room temperature as the coolant, and its cooling water outlet is connected to the water supply inlet of the post-combustion waste heat boiler through a pipeline.
所述的高温机械阀，布置在热解炉布风板以上1～4米的位置，控制从流化床热解炉排出进入流化床半焦加热炉的半焦量，从而与送入流化床半焦加热炉的空气量一起，调节流化床半焦加热炉中加热得到的高温半焦量和温度，最终实现对流化床热解炉中煤热解温度的控制。The high-temperature mechanical valve is arranged at a position 1 to 4 meters above the air distribution plate of the pyrolysis furnace to control the amount of semi-coke discharged from the fluidized-bed pyrolysis furnace into the fluidized-bed semi-coke heating furnace, so as to be connected with the incoming flow Together with the air volume of the fluidized bed semi-coke heating furnace, the amount and temperature of the high-temperature semi-coke obtained by heating in the fluidized bed semi-coke heating furnace are adjusted, and finally the control of the coal pyrolysis temperature in the fluidized bed pyrolysis furnace is realized.
所述的半焦冷却装置，采用室温下的水作冷却剂来冷却半焦，冷却水在将半焦冷却的同时被加热，被加热后的冷却水进一步被送入补燃式余热锅炉中用于生产蒸汽产品。The semi-coke cooling device uses water at room temperature as a coolant to cool the semi-coke, and the cooling water is heated while cooling the semi-coke, and the heated cooling water is further sent to the post-combustion waste heat boiler for use for the production of steam products.
所述的流化床热解炉，运行温度为500～800℃，在500～650℃温度区间运行时焦油相对产率较高，在700～800℃温度区间运行时热解煤气相对产率较高，热解所得到的半焦产品为优质的颗粒状半焦，用途广泛。The fluidized bed pyrolysis furnace has an operating temperature of 500-800°C. The relative yield of tar is relatively high when operating in the temperature range of 500-650°C, and the relative yield of pyrolysis gas is relatively high when operating in the temperature range of 700-800°C. High, the semi-coke product obtained by pyrolysis is high-quality granular semi-coke, which is widely used.
所述的流化床半焦加热炉，是一个绝热炉，炉内所送入的已预热过的空气仅用于燃烧少量半焦将未燃烧半焦颗粒加热到850～1000℃。The fluidized bed semi-coke heating furnace is an adiabatic furnace, and the preheated air fed into the furnace is only used to burn a small amount of semi-coke to heat unburned semi-coke particles to 850-1000°C.
本发明与现有技术相比，具有以下优点：Compared with the prior art, the present invention has the following advantages:
(1)本发明利用流化床煤热解技术，燃烧少量半焦加热半焦为热载体，热解所产煤气和焦油品质好，煤气全部外供作产品，同时可外供优质半焦产品和蒸汽；(1) The present invention uses fluidized bed coal pyrolysis technology to burn a small amount of semi-coke and heat the semi-coke as a heat carrier. The quality of coal gas and tar produced by pyrolysis is good, and all the coal gas is supplied externally as products, and at the same time, high-quality semi-coke products can be supplied externally and steam;
(2)采用高温机械阀，能准确控制送入半焦加热炉的半焦量，从而实现准确调控流化床热解炉中煤热解温度。通过调节煤热解各产品的比例，可实现多联产系统的优化运行，降低投资和生产成本，实现系统整体效益最优化；(2) High-temperature mechanical valves are used to accurately control the amount of semi-coke fed into the semi-coke heating furnace, so as to accurately control the coal pyrolysis temperature in the fluidized bed pyrolysis furnace. By adjusting the proportion of each product of coal pyrolysis, the optimized operation of the polygeneration system can be realized, investment and production costs can be reduced, and the overall benefit of the system can be optimized;
(3)由于半焦加热炉是绝热燃烧炉，同时进入加热炉的空气预先利用烟气余热加热到较高的温度，从而尽量减少用于加热半焦的半焦燃烧量。配置有补燃式余热锅炉生产蒸汽和空气预热器加热空气，能够有效利用半焦加热炉高温烟气的热量，热效率高。(3) Since the semi-coke heating furnace is an adiabatic combustion furnace, at the same time, the air entering the heating furnace is heated to a higher temperature by using the waste heat of the flue gas in advance, so as to minimize the amount of semi-coke combustion used to heat the semi-coke. Equipped with a post-combustion waste heat boiler to produce steam and an air preheater to heat air, it can effectively utilize the heat of the high-temperature flue gas of the semi-coke heating furnace, with high thermal efficiency.
(4)由于热解过程的还原特性，煤中硫、氮有很大一部分转化为易于处理的形式迁移到煤气中，半焦产品中硫、氮含量低，硫、氮污染物排放低。(4) Due to the reducing characteristics of the pyrolysis process, a large part of the sulfur and nitrogen in the coal is converted into an easy-to-handle form and migrates to the gas. The sulfur and nitrogen content in the semi-coke product is low, and the sulfur and nitrogen pollutant emissions are low.
附图说明 Description of drawings
图1是基于流化床热解技术的煤气焦油半焦蒸汽多联产工艺图。Figure 1 is a process diagram of steam polygeneration of gas tar and semi-coke based on fluidized bed pyrolysis technology.
图中附图标记：1给料口，2再循环热解煤气的入口，3高温半焦入口，4流化床热解炉，5出料口，6一级旋风分离器，7二级旋风分离器，8煤气冷却系统，9热解煤气出口，10焦油出口，11炉底半焦排出装置，12半焦冷却装置，13半焦产品出口，14高温机械阀，15第一返料器，16半焦入口，17空气入口，18流化床半焦加热炉，19返料装置，20第二返料器，21一级高温旋风分离器，22二级高温旋风分离器，23补燃式余热锅炉，24高温烟气入口，25空气入口，26空气预热器，27除尘器，28烟气出口。Reference signs in the figure: 1 feeding port, 2 inlet of recirculating pyrolysis gas, 3 inlet of high-temperature semi-coke, 4 fluidized bed pyrolysis furnace, 5 outlet, 6 primary cyclone separator, 7 secondary cyclone Separator, 8 gas cooling system, 9 pyrolysis gas outlet, 10 tar outlet, 11 furnace bottom semi-coke discharge device, 12 semi-coke cooling device, 13 semi-coke product outlet, 14 high-temperature mechanical valve, 15 first return device, 16 Semi-coke inlet, 17 Air inlet, 18 Fluidized bed semi-coke heating furnace, 19 Return device, 20 Second return device, 21 First-level high-temperature cyclone separator, 22 Second-level high-temperature cyclone separator, 23 Supplementary combustion type Waste heat boiler, 24 high-temperature flue gas inlet, 25 air inlet, 26 air preheater, 27 dust collector, 28 flue gas outlet.
具体实施方式 Detailed ways
如附图所示，原料煤通过给料口1加入到流化床热解炉4中，与来自流化床半焦加热炉18的850～1000℃的高温半焦在流化床热解炉4中混合、升温，原料煤发生热解，析出挥发分。析出的挥发分依次经过流化床热解炉4的一级旋风分离器6和二级旋风分离器7分离后进入煤气冷却系统8，在煤气冷却系统8中冷却分离得到焦油和热解煤气。收集到的焦油用于后续加工利用，例如，用来提取单环及多环芳香烃等高附加值产品或通过加氢制取汽、柴油等替代液体燃料，而热解煤气的一部分作为流化介质再循环回流化床热解炉4，净产出的热解煤气经净化后作为化工合成原料或燃气燃料。一级旋风分离器6和二级旋风分离器7分离下来的半焦颗粒直接送入半焦冷却装置12。As shown in the figure, the raw coal is fed into the fluidized
流化床热解炉4内的半焦一部分由高温机械阀14控制从流化床热解炉4一侧的出料口5排出后，经第一返料器15送至流化床半焦加热炉18加热，另一部分半焦则由炉底半焦排出装置11送入半焦冷却装置12，经冷却后作为半焦产品输出用于冶金、燃烧发电、气化制气、活性吸附等。高温机械阀14布置在热解炉布风板以上1～4米的位置，控制从流化床热解炉4排出进入流化床半焦加热炉18的半焦量，从而与送入流化床半焦加热炉18的空气量一起，调节流化床半焦加热炉18中加热得到的高温半焦量和温度，最终实现对流化床热解炉4中煤热解温度的控制。半焦冷却装置12采用室温下的水作冷却剂来冷却半焦，冷却水在将半焦冷却的同时被加热，被加热后的冷却水进一步被送入补燃式余热锅炉23中用于生产蒸汽产品。Part of the semi-coke in the fluidized
进入流化床半焦加热炉18的半焦少量与送入半焦加热炉18的少量空气发生燃烧反应，燃烧所放出的热量用于加热未燃烧的半焦颗粒和烟气。加热后的高温半焦由高温烟气携带依次进入位于流化床半焦加热炉18出口的一级高温旋风分离器21和二级高温旋风分离器22中进行气固分离，分离下来的高温半焦等循环物料经第二返料器20送至流化床热解炉4，为流化床热解炉4中煤热解提供热载体。而分离后的高温烟气携带着少量颗粒，进入补燃式余热锅炉23，在这里与所送入的空气反应，将高温烟气中所含的CO等可燃气体和少量细半焦颗粒等可燃组分进一步燃尽，所产生的高温烟气将从半焦冷却装置12送到补燃式余热锅炉23中已经预热过的水加热为蒸汽，蒸汽用于发电或供热。高温烟气经补燃式余热锅炉23换热后温度有所降低，其后进入空气预热器26，加热空气，加热后的空气分别送入流化床半焦加热炉18和补燃式余热锅炉23提供燃烧所需氧气。经空气预热器26冷却后的烟气经除尘器27除尘后排空。A small amount of semi-coke entering the fluidized-bed
流化床热解炉4的运行温度为500～800℃，在500～650℃温度区间运行时焦油相对产率较高，在700～800℃温度区间运行时热解煤气相对产率较高，可通过调控流化床热解炉4的运行温度来获得不同产率的焦油和煤气产品。流化床热解炉4热解所得到的半焦产品为优质的颗粒状半焦，用途广泛。The operating temperature of the fluidized
流化床半焦加热炉18是一个绝热炉，炉内所送入的已预热过的空气仅用于燃烧少量半焦，将未燃烧半焦颗粒加热到850～1000℃。The fluidized bed
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100641393A CN102585913B (en) | 2012-03-12 | 2012-03-12 | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012100641393A CN102585913B (en) | 2012-03-12 | 2012-03-12 | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102585913A CN102585913A (en) | 2012-07-18 |
| CN102585913B true CN102585913B (en) | 2013-11-06 |
Family
ID=46475155
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012100641393A Active CN102585913B (en) | 2012-03-12 | 2012-03-12 | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102585913B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104132333A (en) * | 2014-08-15 | 2014-11-05 | 中国东方电气集团有限公司 | Fluidized bed semi-coke heat carrier system and method for preventing boiler from being contaminated |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102994126B (en) * | 2012-10-11 | 2014-07-16 | 田原宇 | Pyrolysis upgrading equipment of downward circulating fluidized bed for low-rank coal |
| CN102977924B (en) * | 2012-11-28 | 2014-04-16 | 华东理工大学 | Method for preparing fuel gas by gasifying tanning waste and special equipment |
| CN103031135B (en) * | 2012-12-18 | 2014-07-30 | 中国科学院过程工程研究所 | Fluidized bed hierarchical coal pyrolysis reactor and coal pyrolysis method |
| CN103113905A (en) * | 2013-03-06 | 2013-05-22 | 中煤能源黑龙江煤化工有限公司 | Composite pulverized coal destructive distillation device and method |
| CN103160296B (en) * | 2013-03-29 | 2015-02-25 | 陕西煤业化工技术研究院有限责任公司 | Pyrolysis gasification coupling integrated poly-generation system and process for coal chemical industry |
| CN103436299B (en) * | 2013-09-04 | 2016-01-20 | 马银传 | A kind of biomass fuel solid/liquid/gas reactions producer |
| CN104449774B (en) * | 2014-11-07 | 2017-02-15 | 王树宽 | Down-flow gas semi-coke activated pulverized coal pyrolysis system and method |
| CN104789245B (en) * | 2015-04-07 | 2017-12-05 | 太原理工大学 | A kind of pyrolysis gasifying device and technique |
| CN104946282B (en) * | 2015-06-15 | 2017-05-31 | 宋军 | A kind of handling process of smalls |
| CN105709710A (en) * | 2016-03-03 | 2016-06-29 | 北京清新环境技术股份有限公司 | Multilayer fluidized bed parsing device for conducting pneumatic material return through row tube type heat exchange and coupling of molten salt |
| CN107794069A (en) * | 2016-08-28 | 2018-03-13 | 何巨堂 | The segmentation air-burn process of system is burnt in a kind of pyrolysis of powder containing carbon hydrogen element |
| CN107936992A (en) * | 2017-12-22 | 2018-04-20 | 北京神雾电力科技有限公司 | A kind of high temperature three-segment formula waste heat recovery pyrolysis reactor |
| IT201800003238A1 (en) * | 2018-03-02 | 2019-09-02 | Ambiente E Nutrizione Srl | Process and system optimized for the production of a heated fluid by burning a fuel |
| DE102018133529A1 (en) * | 2018-12-21 | 2020-06-25 | Siqens Gmbh | Burner system and method for providing thermal energy |
| CN115141658B (en) * | 2021-09-18 | 2025-03-18 | 新能能源有限公司 | A pulverized coal hydrogenation gasifier and slag removal method thereof |
| CN114381305A (en) * | 2022-01-20 | 2022-04-22 | 浙江大学 | A dual fluidized bed material circulation control system and control method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4198273A (en) * | 1976-07-28 | 1980-04-15 | Wintershall Aktiengesellschaft | Apparatus for producing petroleum coke calcinate |
| AU4914490A (en) * | 1989-02-06 | 1990-08-09 | L. & C. Steinmuller G.M.B.H. | A device for drying, milling and burning of high ash fuels |
| CN1062751A (en) * | 1992-02-18 | 1992-07-15 | 北京水利电力经济研究所 | A kind of method and device of producing dry distillation gas |
| GB2350370A (en) * | 1999-05-27 | 2000-11-29 | Technip Benelux B V | Process and device for autothermic gasification of solid fuels |
| CN101412915A (en) * | 2008-11-21 | 2009-04-22 | 中国林业科学研究院林产化学工业研究所 | Interior heating type method for continuously preparing coal gas by pyrolysis and gasification of biomass and pyrolysis gasification furnace |
| CN101691501A (en) * | 2009-09-30 | 2010-04-07 | 浙江大学 | Coal-grading conversion poly-generation device and method for producing coal gas, tar and carbocoal on circulating fluid bed |
| CN102031128A (en) * | 2009-09-30 | 2011-04-27 | 中国科学院工程热物理研究所 | Coal gas-tar-semicoke cogeneration method |
-
2012
- 2012-03-12 CN CN2012100641393A patent/CN102585913B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4198273A (en) * | 1976-07-28 | 1980-04-15 | Wintershall Aktiengesellschaft | Apparatus for producing petroleum coke calcinate |
| AU4914490A (en) * | 1989-02-06 | 1990-08-09 | L. & C. Steinmuller G.M.B.H. | A device for drying, milling and burning of high ash fuels |
| CN1062751A (en) * | 1992-02-18 | 1992-07-15 | 北京水利电力经济研究所 | A kind of method and device of producing dry distillation gas |
| GB2350370A (en) * | 1999-05-27 | 2000-11-29 | Technip Benelux B V | Process and device for autothermic gasification of solid fuels |
| CN101412915A (en) * | 2008-11-21 | 2009-04-22 | 中国林业科学研究院林产化学工业研究所 | Interior heating type method for continuously preparing coal gas by pyrolysis and gasification of biomass and pyrolysis gasification furnace |
| CN101691501A (en) * | 2009-09-30 | 2010-04-07 | 浙江大学 | Coal-grading conversion poly-generation device and method for producing coal gas, tar and carbocoal on circulating fluid bed |
| CN102031128A (en) * | 2009-09-30 | 2011-04-27 | 中国科学院工程热物理研究所 | Coal gas-tar-semicoke cogeneration method |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104132333A (en) * | 2014-08-15 | 2014-11-05 | 中国东方电气集团有限公司 | Fluidized bed semi-coke heat carrier system and method for preventing boiler from being contaminated |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102585913A (en) | 2012-07-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102585913B (en) | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology | |
| CN106753489B (en) | A coal pyrolysis steam, tar and gas co-production system and process based on pulverized coal furnace | |
| CN101024782B (en) | Dense phase transport bed coal pressure gasification device and method | |
| CN101691501B (en) | Coal-grading conversion poly-generation device and method for producing coal gas, tar and carbocoal on circulating fluid bed | |
| CN103320175B (en) | High-efficiency clean low-carbon coal graded utilization method and device | |
| CN103756731B (en) | A kind of reciprocating cycle double fluidized bed solid fuel gasification device and method | |
| CN102533296B (en) | Oil shale rotary kiln dry distillation and circulating fluidized bed combustion process | |
| CN101818073B (en) | Dry distillation and semicoke incineration integrated system for oil shale | |
| CN102031133B (en) | Device and method for producing biological fuel oil by quickly cracking biomass | |
| CN202203950U (en) | Organic solid waste pyrolyzation and gasification device | |
| CN101245264A (en) | Single-bed self-heating pyrolysis gasification combustion reactor and pyrolysis gasification combustion method | |
| CN204874397U (en) | Three fluidized bed solid thermal carriers pyrolysiss of coal gasification oxygen boosting burning cascade utilization device | |
| CN101747918A (en) | Method for preparing natural gas by dry quenching co-production coal | |
| CN103146432A (en) | Biomass pyrolysis gasification and tar catalytic cracking device and method | |
| CN103031135B (en) | Fluidized bed hierarchical coal pyrolysis reactor and coal pyrolysis method | |
| CN105062528A (en) | Coal-pyrolysis polygeneration process and device applicable to pulverized coal furnace | |
| CN102977903B (en) | Low-rank coal downward circulating fluidized bed pyrolysis quality improvement process | |
| CN105295982B (en) | The Poly-generation utilization system and its technique of a kind of oil shale attendants | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN107043641A (en) | Circulation fluidized bed coal gasifying method and device with fine ash loopback | |
| CN116716128A (en) | Preheated gasification method and device | |
| CN108048138A (en) | Based on the double-fluidized-bed biomass graded conversion of middle low temperature and coal-burning boiler coupled electricity-generation method and its system | |
| CN201517093U (en) | Circulating fluidized bed coal grading conversion coal gas tar semi-coke poly-generation device | |
| CN100363461C (en) | A method and device for producing gas by twin-bed pyrolysis of biomass/domestic waste | |
| CN105087025A (en) | Moving bed coal pyrolysis based polygeneration device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |