200946668 六、發明說明： 【發明所屬之技術領域】 、本發明係關於一種在壓力氣化法中向一加壓饋料槽中 以受控連續方式供應細粒狀至經粉碎燃料材料之方法，其 中細粉狀或經粉碎（<0·5 mm)的諸如煤、石油焦、生物 廢料或燃料的燃料材料係藉由在高於爐渣熔點之溫度於高200946668 VI. Description of the Invention: [Technical Field] The present invention relates to a method for supplying fine-grained to pulverized fuel material in a controlled continuous manner in a pressurized feed tank in a pressure gasification process, A finely powdered or pulverized (<0.5 mm) fuel material such as coal, petroleum coke, biological waste or fuel is at a temperature above the melting point of the slag.
壓下與含氧氣化劑反應而轉變成具有低微粒負荷“Μ kg/m3 ;無流化床）之懸浮液。 在壓力氣化法之過程中，含碳燃料材料係藉助於含氧 氣體而轉化’其中該含氧氣體以低於化學計#之比率供 應，從而獲得含有一氧化碳之產物氣體。若反應氣體含有 水蒸汽，則產物氣體具有合成氣體特徵且大部分含有氫 氣。為在低於化學計量之條件下達成儘可能完全的轉化， 燃料材料必須以細粉狀狀態饋人反應器中。反應通常在高 壓下發生。 由於氣化反應僅在連續操作一段延長時間時才能經濟 地操作，因11匕♦時間單位所供應之細粉狀燃料材料之量應 儘可犯匣疋以確保無故障操作。燃料材料至所需壓力位準 之傳遞及燃料材料在壓力下之供應為煤氣化反應中仍有待 解決之問題。為此’煤的氣化設備始終包括用以確保向反 應器無故障供應燃料之設備裝備。該裝備通常由重力流操 作之專用配料槽與閉鎖料斗總成組成。 使用配料槽並非始終為完全消除裝載反應器時發生之 壓力變化的方式。此可能在碳的氣化反應期間壓力導致變 5 200946668 化’而壓力變化將暫時改變合成氣體之組成。特別是，從 壓力栓不連續地填充配料槽會產生壓力變化，此變化對用 作供配料槽與燃燒器之間的輸送用之驅動力的壓力差具有 不利作用。 备向煤氣化反應供應燃料材料時所進行之以重力流 引入燃料材料亦為可能的誤差來源。由於細粉狀燃料材料 視其品質及乾燥程度而定可能會阻塞或堵塞，因此輸送有 時僅將分批進行或意外地週期性中斷。另外，基於重力流 之閉鎖料斗系統常常需要複雜的設計方案，此係由於之間 有待達成輸送之槽必須排列於彼此頂部。 根據現有技術之燃料饋料系統為支出密集型的且操作 上並非始終可靠。在大容量設備之狀況下礙磨單元與氣 化單70的空間分離涉及關於細粉狀燃料材料自碾磨單元傳 送至燃料饋料系統的大量額外支出。這使得必須提供額外 的裝傷（輸送容器或氣動泵、過濾器、饋料系統上方之緩 衝罐）。另外，管道鋪設、儀錶化及建造工作衍生大量支出， 建造作係、因為在1化單元的最高高度處之緩衝罐的暴露 位置而尤其導致大量支出。此外，已證實根據重力流原理 操作之閉鎖料斗系統操作上並不充分可靠。額外裝備不管 怎樣皆會增加故障風險。 除此通常已知之事實以外，閉鎖料斗的重力饋料原理 涉及特定功能性風險。儘管存在許多極不同方法，但已證 實足夠小心地進行容器加壓法以保持散裝材料之内應力足 夠低係極為困_。在許多狀況下，散裝材料被局部壓實至 200946668 -定程度，以使得隨後完全不會引發或僅以不足程度引發 至饋料槽的重力流。因此，饋料槽之固體材料存貨減少， 這常常引起輪出受到限制或甚至可能弓，起氣化單元故障。 若歸因於設備之高容量的尺寸過大遭遇到與構造的限 制且若氣化單元要針對高於已操作多年之單元虔力（一般 為2.5MPa)的壓力（―般為4Μρ〇進行設計的話，則問 題就會加劇。 〇 ㈣成所需的重力流，則從閉鎖料斗至饋料槽中之閉 2料斗重力饋料將產生極高傳遞質量流率且因此實現相 2短的傳遞期。閉鎖料斗饋料期間的固體傳遞將使饋料槽 ==面升高。填料水平面接著將因向燃燒器供應之 =量而再次連續降低，且因下一個閉鎖料斗傳遞操作而 再-人升尚。以此方式’饋料槽經受暫時改變之條件 至可能影響來自饋料槽的穩定運送。保持麼力條件、填料 =面及偶入一叫材料以脈衝方式饋入散裝填料 ❾巾（例如）儘可能關於時間為㈣的係_更加有利。 本發明藉由一種配料槽而解決這些問題，該配料槽在 壓力下含有細粉狀燃料材料，且根據本發明具有幾乎 填料水平面。根據本發明，藉由從至少兩個閉鎖料 線Li) 一個聯合使用之適於密集流輸送之連續供應管 線來連續供應固體材料，係確保饋料槽中幾乎怪定 水平面。由於連續供應管線並非由重力操作，因、 =饋料槽及供應閉鎖料斗安裝於不同測地高度處， 外女裝成彼此距離較大，如可例如於不同建築物卜 7 200946668 【先前技術】 已知用於燃料材料之配料裝置，其將燃料材料經由一 具有上游閉鎖料斗系統之配料槽饋入反應器中。us 5143521 A描述將燃料材料饋入饋料槽中之系統，該饋料槽 儲存加壓燃料材料且由一閉鎖料斗系統連續供應有細粉狀 燃料材料。該等閉鎖料斗係由管線連接且交替加壓。可經 由膨脹式渦輪、文氏管（Venturi tube )及壓縮機之系統使 用一個閉鎖料斗之膨脹氣體的壓力，以加壓另一個閉鎖料 斗。以此方式，有可能在大氣壓條件下將細粉狀煤之壓力 調整至適於煤氣化之位準。氮氣係用作加壓氣體。 DE 102005047583 A1描述在壓力下向一煤氣化反應器 配料且饋送粉碎燃料材料之方法及設施。為確保燃料材料 至煤氣化反應器之饋料經過一段給定時間是恆定的，將燃 料係在中間儲存於一配料槽中，在該配料槽之下部中，藉 由饋入氣體而在槽底部上方產生一密集流化床，經過該流 化床，粉碎燃料材料係經由燃燒器而被連續供應至一加磨 氣化反應器。此處，向燃燒器的實際饋入係藉由所謂高速 輸送來實施，纟中供應到燃燒器下游之饋料管線的輔助氣 想係用於產生麼力|，燃料材料接著係藉此M力差被傳輸 至燃燒器。從兩個栓將燃料材料供應到配料槽，該等拴藉 助於重力及-星式㈣器將燃料材料傳輸至配料槽中。然 而’這容易故障且需要高程結構。碾磨裝置的使用未提及。 【發明内容】 藉助於合 本發明描述用於將含碳燃料材料研成粉末 200946668 適氣體對燃料加壓、將燃料分散並運送至饋料槽且將其饋 入反應器中的整合式方法。在所謂連續供應管線中，藉由 密集流輸送來實施燃料的傳輸、分散及饋人反應器中。以 此方式反應器之完整燃料供應鏈可在沒有重力流下進 行。氣化反應器的出口溫度較佳地是高於测七與2峨 之間的範圍内的爐㈣點’且壓力較佳的是介力〇 3奶 與8 MPa之間。 纟此责景之下’密集流輸送表示氣動輸送，其並不會 將燃料材料微粒當做個別微粒傳輸，而是以填充管道整個 橫截面積的密集密封材料或填料形式的密集流傳輸。密集 流輸送之流率-般介於4_與5 _之間，其中儘管氣流 之固體負荷高，但仍達成高傳輪體積。密集流輸送之特徵 在於平緩傳輸材料及特別是幾乎不易於因黏附或濕輸送材 料而故障。本發明的氣動式密集流輸送法較佳以至少_ k*3之固體密度及在至少〇_5巴（W)之差力壓下進行。 ❹ 肖別技術方案係針對向-已冷卻的反應器（15)供應 細粉狀燃料材料，用於藉助於含氧氣化劑在壓力下氣化之 方法，其中： 12〇〇°C與2000°C之間的範 MPa與8 MPa之間， •氣化器出口溫度高於介於 圍内之爐渣熔點且壓力介於〇.3 拾系統加壓至高於氣化 個饋料槽且自彼處以密 一或數個氣化器之一或 •且該細粉狀燃料材料經由_ 器壓力之壓力位準，傳遞至至少_ 集流經由至少一個燃料管線配料至 多個氣化燃燒器中，且 200946668 •從至少兩個閉鎖料斗到至少一個饋料槽之傳遞係藉 由使用一氣動連續供應管線以至少100 kg/m3之固體材料密 度及至少〇.5巴之差力壓聯合、同時或連績地進行。 在該方法之具鱧實例中，藉著至少一個連接裝置及至 >一個一體化疋件來控制從閉鎖料斗至饋料槽之傳遞且 藉助於個別連接裝置或藉助於具有傳遞連接裝置之額外一 趙化/0件來實施自一體化元件至饋料槽之傳遞。 傳遞連接裝置以例示性方式設計為適於密集流輸送之 連續供應管線。藉由在閉鎖料斗下游安裝—體化元件，將 燃料材料係從閉鎖料斗經由許多連續供應管線而被輸送至 饋料槽’管線數目小於閉鎖料斗數目。亦有可能引導來自 閉鎖料斗出口之固體材料不是直接、而是經由連接元件進 入一體化元件中，使得其首先經由管線傳入一體化元件中 且接著傳入連續供應管線中。此處，一體化元件之數目小 於閉鎖料斗之數目，且可與連續供應管線之數目相同。_ 體化7〇件儘可能接近出口喷嘴而提供，且儘可能與其對稱 排列以確保平穩固體流。 在該方法之較佳具體實例中，將燃料材料藉助於研磨 機或合適碾磨裝置處理成細粉狀形式。為此目的，燃料材 料可以用任何形式獲得。有可能運送已呈細粉狀之燃料材 料。在該狀況下，技術方案僅針對燃料材料加壓及傳輸至 反應器中。然而，碾磨法通常為本發明方法之不可或缺的 部分’若碾磨裝置以局部接近反應器排列則尤其如此。在 本發明之較佳具體實例中，煤研磨及乾燥（CMd )單元為 200946668 煤氣化設#之不可或缺的部分。 可使:til功能’將閉鎖料斗以氣體加壓。舉例而言， 惰性氣體“之處理氣體。亦有可能使用惰性氣體。以 再循環氣發來有利丄藉助於 程，在由所供應之氣體對閉鎖料斗加塵2式:己置傳遞過 斗之相互部分加屢。為保持處理條件儘=、订閉鎖料 料斗交替加壓及減壓。 ’、 旎恆定，將閉鎖 在該方法之另一具體實例中 蓋且為以惰性氣體覆蓋經惰性氣體覆 -氣體。將閉鎖料斗以規律的:間=閉:料斗之膨 過程Ϊ择^所排放之氣體可再循環至碌磨裝置。此將使 下Μ 1可靠且將設備操作成本料於合理程度以 ^另外，將礙磨迴路之氣體除塵。為此目的，使用一於 加其亦可用於將來自閉鎖料斗之膨脹氣體除塵： :壓或膨脹氣體可藉助於一基本上處於過 塵分離器除塵。 j位置之粉 接著較佳將細粉狀燃料材料饋入一饋料槽中。以此方 ^ ’有可能根據可用性來錯存燃料材料，且可能暫時地緩 原料流。因此有可能調整航頸狀態，其藉由曰後再填 而受到補償。 ' 為進行本發明之方法，可藉由研磨或碟磨而分成小微 拉的所有固體含碳燃料材料皆可使用。此等材料尤A可為 所有種類之碳，其中硬煤、褐煤及基本上所有碳化種類之 200946668 煤皆適合。諸如木材、生物燃料及其他諸如塑膠廢物及石 由焦的燃料材料或其混合物之生物燃料材料亦適合作燃料 ；為進行本發明之方法，應僅可能將燃料材料壓碎成 適合於密集流輸送之細粉狀形式。 在磨碎過程及在饋料槽中儲存之後，將固鱧材料傳至 鎖料斗系統’在該閉鎖料斗系統中以所供應之氣體對固 料力壓以進行氣化反應。在本發明之較佳具體實例Pressing a reaction with an oxygenating agent to convert into a suspension having a low particulate loading of "Μ kg/m3; no fluidized bed." During the pressure gasification process, the carbonaceous fuel material is by means of an oxygen-containing gas. Conversion 'where the oxygen-containing gas is supplied at a ratio lower than the stoichi# to obtain a product gas containing carbon monoxide. If the reaction gas contains water vapor, the product gas has a characteristic of a synthesis gas and most contains hydrogen. The metering conditions are as complete as possible, and the fuel material must be fed to the reactor in a finely powdered state. The reaction usually takes place under high pressure. Since the gasification reaction can only be operated economically for a prolonged period of continuous operation, 11匕♦ The amount of finely powdered fuel material supplied by the time unit should be as ridiculous as possible to ensure trouble-free operation. The transfer of fuel material to the required pressure level and the supply of fuel material under pressure are in the coal gasification reaction. There are still problems to be solved. For this reason, the coal gasification equipment always includes equipment and equipment to ensure trouble-free supply of fuel to the reactor. The special dosing tank operated by the gravity flow is composed of the lock hopper assembly. The use of the dosing tank is not always a way to completely eliminate the pressure change that occurs when the reactor is loaded. This may cause pressure during the gasification reaction of carbon. The pressure change temporarily changes the composition of the synthesis gas. In particular, the pressure change is generated by the pressure plug being discontinuously filled in the batching tank, and this change is used as the pressure difference between the driving force for conveying between the batching tank and the burner. It has an adverse effect. The introduction of fuel material into the coal gasification reaction by gravity flow is also a possible source of error. Since fine powdered fuel materials may block or clog depending on their quality and dryness, Conveying can sometimes only be done batchwise or accidentally periodically. In addition, gravity flow based lock hopper systems often require complex designs, since the grooves to be transported between them must be arranged on top of each other. The fuel feed system is cost intensive and not always reliable in operation. The spatial separation of the obstruction unit from the gasification unit 70 in the case of a quantity of equipment involves a large additional expenditure on the transfer of finely powdered fuel material from the milling unit to the fuel feed system. This necessitates the provision of additional injuries (transport containers or Pneumatic pumps, filters, buffer tanks above the feed system. In addition, pipeline laying, instrumentation and construction work generate a large amount of expenditure, construction, because of the exposure position of the buffer tank at the highest height of the unit In addition, it has been proven that the locking hopper system operating according to the gravity flow principle is not sufficiently reliable in operation. Additional equipment increases the risk of failure anyway. In addition to the generally known facts, the gravity feeding principle of the locking hopper involves Specific functional risks. Although there are many very different methods, it has proven to be sufficiently careful to carry out the container pressurization method to keep the internal stress of the bulk material low enough. In many cases, the bulk material is partially compacted to 200946668. - a degree so that it is not triggered at all or is only triggered to the feed Gravity flow. As a result, the stock of solid material in the feed chute is reduced, which often causes the wheel to be restricted or even possible to bow, causing the gasification unit to fail. If the size of the high capacity due to the equipment is too large, it is limited by the construction and if the gasification unit is designed for a pressure higher than the unit pressure (usually 2.5 MPa) that has been operated for many years ("typically 4 Μ 〇") The problem is exacerbated. 〇 (d) into the required gravity flow, the closed 2 hopper gravity feed from the lock hopper to the feed trough will produce a very high transfer mass flow rate and thus achieve a short phase 2 transfer period. The solids transfer during the feed of the lock hopper will cause the feed chute == face to rise. The fill level will then continue to decrease again due to the amount of supply to the burner, and will continue to be lifted due to the next lock hopper transfer operation. In this way, the feed chute is subjected to temporary changes to conditions that may affect stable transport from the feed chute. Maintaining force conditions, packing = face and occasional material is pulsed into the bulk packing wipe (for example) It is more advantageous to have as much as possible the time (4). The invention solves these problems by means of a dosing tank which contains a finely powdered fuel material under pressure and which has almost a filler according to the invention Plane. According to the present invention, by) from a combined use of at least two feed lines Li of the latch is adapted to supply a continuous mass flow of the conveying pipeline to a continuous supply of solid material in the feed trough drivetrain strange almost constant level. Since the continuous supply line is not operated by gravity, the =, feed trough and supply lock hopper are installed at different geodesic heights, and the outer wears are at a greater distance from each other, as can be, for example, in different buildings. 7 200946668 [Prior Art] Known as a dosing device for fuel materials, the fuel material is fed into the reactor via a dosing tank having an upstream lock hopper system. Us 5143521 A describes a system for feeding fuel material into a feed trough that stores pressurized fuel material and is continuously supplied with finely powdered fuel material by a lock hopper system. The lock hoppers are connected by lines and alternately pressurized. The pressure of the inflation gas of a lock hopper can be used by the system of the expansion turbine, the Venturi tube and the compressor to pressurize the other lock hopper. In this way, it is possible to adjust the pressure of the fine powder coal to a level suitable for coal gasification under atmospheric pressure. Nitrogen is used as a pressurized gas. DE 102005047583 A1 describes a method and a facility for dosing and feeding a pulverized fuel material under pressure into a coal gasification reactor. In order to ensure that the feed of fuel material to the coal gasification reactor is constant over a given period of time, the fuel is stored in a batching tank in the middle, in the lower part of the batching tank, by feeding the gas at the bottom of the tank A dense fluidized bed is created above, through which the pulverized fuel material is continuously supplied to a gasification reactor via a burner. Here, the actual feed to the burner is carried out by means of so-called high-speed transport, the auxiliary gas supplied to the feed line downstream of the burner is intended to be used to generate the force |, and the fuel material is then used for this force. The difference is transmitted to the burner. Fuel material is supplied from the two plugs to the batching tank, which transfers the fuel material to the batching tank by means of gravity and a star (four). However, this is easy to malfunction and requires an elevation structure. The use of a milling device is not mentioned. SUMMARY OF THE INVENTION An integrated method for pressurizing a carbonaceous fuel material into a powder by means of a suitable gas pressurizing, transporting and transporting the fuel to a feed trough and feeding it into a reactor is described. In a so-called continuous supply line, the transport, dispersion and feeding of the fuel are carried out by means of dense flow transport. In this way the complete fuel supply chain of the reactor can be operated without gravity flow. The outlet temperature of the gasification reactor is preferably higher than the furnace (four) point in the range between seven and two, and the pressure is preferably between between 3 and 8 MPa. Under this circumstance, 'dense flow transport means pneumatic transport, which does not transmit fuel material particles as individual particles, but rather dense flow in the form of dense sealing materials or fillers that fill the entire cross-sectional area of the pipe. The flow rate of dense flow transport is generally between 4 and 5 _, although a high transfer volume is achieved despite the high solids loading of the gas stream. Dense flow transport is characterized by a gentle transfer of material and, in particular, little difficulty in failure due to adhesion or wet transport material. The pneumatic dense flow transport method of the present invention is preferably carried out at a solid density of at least _k*3 and at a differential pressure of at least 〇5 bar (W). ❹ The Xiaobiao technical solution is for supplying a finely powdered fuel material to a cooled reactor (15) for gasification under pressure by means of an oxygenating agent, wherein: 12 ° C and 2000 ° Between the MPa and 8 MPa between C, • The gasifier outlet temperature is higher than the slag melting point and the pressure is between 〇.3 The pick-up system is pressurized above the gasification feedlot and from One or a plurality of gasifiers or one and/or the finely pulverized fuel material is transferred to at least _ current collecting via at least one fuel line to a plurality of gasification burners via a pressure level of _ pressure, and 200946668 • The transfer from at least two lock hoppers to at least one feed trough is achieved by using a pneumatic continuous supply line with a density of solid material of at least 100 kg/m3 and a differential pressure of at least 55 bar, simultaneous or continuous performance Conducted. In an exemplary embodiment of the method, the transfer from the lock hopper to the feed chute is controlled by at least one connecting device and to an integrated element and by means of an individual connecting device or by means of an additional one having a transfer connection Zhao Hua / 0 pieces to implement the transfer from the integrated component to the feed trough. The transfer connection device is designed in an exemplary manner as a continuous supply line for dense flow transport. By installing the body-forming elements downstream of the lock hopper, the fuel material is delivered from the lock hopper to the feed trough via a plurality of continuous supply lines. The number of lines is less than the number of lock hoppers. It is also possible to direct the solid material from the outlet of the lock hopper not directly, but into the integrated element via the connecting element, such that it is first introduced into the integrated element via the line and then into the continuous supply line. Here, the number of integrated components is less than the number of latching hoppers and may be the same as the number of continuous supply lines. _ The body 7 pieces are provided as close as possible to the outlet nozzle and are arranged as symmetrically as possible to ensure a smooth solid flow. In a preferred embodiment of the method, the fuel material is processed into a fine powder form by means of a grinder or a suitable milling device. For this purpose, the fuel material can be obtained in any form. It is possible to transport fuel materials that have been finely powdered. In this case, the technical solution only pressurizes and transports the fuel material into the reactor. However, the milling process is generally an integral part of the process of the invention, especially if the milling device is partially adjacent to the reactor. In a preferred embodiment of the invention, the coal grinding and drying (CMd) unit is an integral part of 200946668 Coal Gasification. The til function can be used to pressurize the lock hopper with gas. For example, the inert gas "process gas. It is also possible to use an inert gas. It is beneficial to use the recirculating gas to facilitate the use of the gas. The gas is supplied to the lock hopper by the supplied gas. In order to maintain the processing conditions, the processing conditions are kept as follows, and the lock hopper is alternately pressurized and depressurized. ', 旎 is constant, and the cover is blocked in another specific example of the method and covered with an inert gas over the inert gas. - gas. The locking hopper is regularly: the = clogging process: the venting process can be recycled to the honing device. This will make the squat 1 reliable and the equipment operating cost is reasonable. In addition, the gas impeding the circuit is dedusted. For this purpose, it can also be used to dedust the expanding gas from the lock hopper: the pressure or expansion gas can be dedusted by means of a substantially dust separator. The powder at the j position is then preferably fed into the feed trough in a fine powdered fuel material. It is possible to misplace the fuel material depending on the availability, and may temporarily slow the flow of the material. Therefore, it is possible to adjust The neck state, which is compensated by refilling the crucible. 'To carry out the method of the present invention, all solid carbonaceous fuel materials which can be divided into small micro-drawings by grinding or disc grinding can be used. It can be suitable for all types of carbon, including hard coal, lignite and substantially all carbonized types of 200946668 coal. Biofuel materials such as wood, biofuels and other fuel materials such as plastic waste and stone coke or mixtures thereof are also suitable. For the purpose of carrying out the method of the present invention, it is only possible to crush the fuel material into a fine powder form suitable for dense flow transport. After the grinding process and storage in the feed trough, the solid material is transferred to the lock. The hopper system 'in the lock hopper system presses the solids force with the supplied gas for gasification reaction. In a preferred embodiment of the invention
績料槽處於大氣麼下。藉著重力能有利地進行固體材 料向閉鎖料斗中之輸送。 、、進行本發B月之方法，閉鎖料斗系統由至少兩個閉鎖 料斗組成。以此方式’有可能以串聯方式連接排放操作， 且確保幾乎連續之材料流。在有利具體實例中閉鎖料斗 係被個別地加魔。 在本發明方法之具體實例中，使用兩個閉鎖料斗以確 續材料流。設備之投資成本因此較低。在本發明之另The performance tank is in the atmosphere. The transport of solid material into the lock hopper is advantageously carried out by gravity. The method of the present invention is performed by the method of the present invention. The lock hopper system is composed of at least two lock hoppers. In this way it is possible to connect the discharge operation in series and to ensure an almost continuous flow of material. In an advantageous embodiment, the locking hopper is individually enchanted. In a specific embodiment of the method of the invention, two lock hoppers are used to ensure material flow. The investment cost of equipment is therefore lower. Another in the present invention
^體實例中，亦可能使用三個或三個以上閉鎖料斗。此 在同设備產量之狀況下尤其受推薦。 有可能使用複數個閉鎖料斗及複數個—趙化元件。 :二：本發明之設施可由任何數目之閉鎖料斗及一趙化 =。閉鎖料斗數目由設備產量決定。-趙化元件數 =鎖料斗數目及連續供應管線數目決定。理論上任何 不同排列皆為可能的。基本上亦可視需H# 與—駚儿_ w J优萬要將閉鎖料 置 "°、互相連接。為此’可使用任何數目之連接 。佳的連接裝置為管線。亦可能為例如軟管或凸緣 12 200946668 亦可視需要選擇空間的互相連接模式。 在對槽加虔之後，將所含有之燃料材料以配料的量排 出，及接著使槽中之壓力膨脹。在本發明之有利具趙實例 中，使用膨脹氣體對循環中的下一閉鎖料斗部分地加麼。 為了改良功效，此可藉由將膨服氣體直㈣人待加I之槽 中來實施。 為降低膨脹氣體之粉塵負荷，有利地將膨服氣體引入 〇粉塵分離器中，該粉塵分離器亦用於將來自儲存槽或來自 礙磨過程之氣體除塵。原則上，亦有可能藉助於若干獨立 粉塵分離器從氣體清除固體材料粉塵。為保持低投資成 本，僅使用一個粉塵分離器為有利的。 將來自閉鎖料斗的材料流係經由至少一個一體化元件 及連續供應管線送至饋料槽。為利用本發明的優點，閉鎖 料斗係以達成至饋料槽是幾乎連續之燃料材料流的方式相 繼清空。以此方式，可向氣化反應器之後續饋料槽供應具 〇 有適合於氣化反應之壓力的連續材料流，其中饋料槽之填 料水平面保持幾乎怪定。可根據方法之有利具體實例來調 整饋料槽中燃料材料之填料水平面，使得其經過一段給定 時間變化不超過± 30%。若本發明之方法係由專業人員進 行，則有可能容易地將饋料槽之填料水平面在經過一段延 長時間的變化保持於不超過±丨0〇/〇之範圍内。 亦可藉由調整閉鎖料斗與饋料槽之間的壓力差來控制 來自閉鎖料斗之細粉狀燃料材料的連續供應，保持饋料槽 之填料水平面恆定。進入閉鎖料斗之自由空間中的氣體入 13 200946668 σ或出〇會影響閉鎖料斗與饋料槽之間的壓力差且被用作 固艘材料傳輸之控制參數。 為進行該方法，細粉狀燃料材料較佳具有小於 0.5 mm 之粒度。此係以碾磨及磨碎處理而達成。可藉由在緊鄰排 放喷嘴處向閉鎖料斗中添加氣體而促進固鳢材料從閉鎖料 斗排放》藉由向連續供應管線中或向一體化元件中或向兩 者中添加氣體，有可以利地調整連續供應管線令之密度。 在此點處添加氣趙亦可用來淨化連續供應管線或一體化元 亦可向介於閉鎖料斗與一體化元件之間的連接元件供 ❹ 應氣體。 在本發明之有利具體實例中，在 装2送氣艘趙積係被回收於饋料槽中且藉助於一注入 進㈣=回至閉鎖料斗中。返回之輸送氣趙與注入器之推 用，且共同地被當做用於放空閉鎖料斗的置換氣體使 亦用於在輸送過程令維持閉鎖料斗壓力。 為符合某也要炎 ^ ❹ 斗將固體材料；時戈㈣ ，兩個或兩個以上閉鎖料 閉鎖料斗之間二 排放至輸送管線中。可藉著 氣趙平衡。 帛連接管線來有利地達成饋料斗之間的 本發明之方法亦可包 續方法的方法。本發明之方之煤氣化方法之後 所需之方法步驟。此等 2包括反應器的常規操作 步驟亦可為諸如供應用於教二(：如）清潔步驟… 驟。亦可能為量測諸‘接鬆散填料之氣體的支持方法步 料位準、流率、麼力或溫度之參 14 200946668 、法步驟。本發明尤其亦描述一種進行此方法之設 施。本發明之設施可包括根據本發明之方法操作一煤氣化 設備所需的所有設備單元。 技術方案亦針對用於向一供固體燃料材料氣化用之反 應器供應固體燃料材料之設施，其包含： 一碾磨裝置， 一粉塵分離器， ❿ ❹ 一儲存槽， 至少兩個閉鎖料斗， 至少一個用於密集流輸送的連接裝置， 一饋料槽， 一氣化反應器，其中： 該礙磨裝置係藉助於連接裝置而連接至一儲存容 器中粉塵分離器安裝於該礙磨裝置與該儲存槽之 間，且 •該儲存容器係經由適於重力流或密集流輸送之連接 裝置而連接至該等閉鎖料斗，且 •該等閉鎖料斗係藉助於共同使用之適於作密集流輸 送之連續供應管線的連接裝置而連接至一饋料槽，且此饋 料槽係經由其他燃料材料管線而連接至該氣化反應器。 從閉鎖料斗系統至饋料槽之密集流輸送允許將饋料槽 安裝在與閉鎖料斗系統相同或不同的測地高度處。在目前 已知之重力閉鎖料斗系統的狀況下，將閉鎖料斗安裝於饋 料槽上方為必不可少的。藉由此措施，有可能使總體設備 15 200946668 之構造高度降至相當大的程度。亦有可能將閉鎖料斗系統 及饋料槽及反應器定位於分開的建築物中。本發明亦涉及 針對各別單元可選擇較低構造高度之優點。各種設備組件 可視需要加以排列，使得可以靈活方式進行設備的空間布 局0 燃料材料從閉鎖料斗至饋料槽的傳遞係經由至少一個 連接裝置及至少-個-體化元件實&，域一體化元件至 饋料槽的傳遞係經由密集流輸送之個別連續供應管線來實 施。自閉鎖料斗至饋料槽的傳遞可經由具有傳遞連接裝置 之其他一體化元件來實施。 視該方法之具體實例而定，使用兩個或兩個以上閉鎖 料斗對燃料材料加壓。料具有高燃料材料處理能力之設 傑或若閉鎖料斗系統要被加愿至較高壓力，則這是特別推 :的。閉鎖料斗之入口側連接至一饋料槽，該饋料槽藉助 ;密集流輸送與重力輸送二者將燃料材料輸送至閉鎖料斗 :二為此目的，可在儲存槽與閉鎖料斗之間的合適位置安 :星式饋料器或一材料歧管。亦有可能在儲存槽與閉鎖 枓+之間安裝中間容器、球形容器或氣體饋入裝置。 備的燃料材料供應系統亦可包括任何所需類 的碟磨裝置或研磨機。研磨機繼而亦可包括其他磨碎裝 置，諸如木材用撕碎機或煤用麼碎機。亦可向 氣趙或將其以惰性氣想覆[在本發明設施之較 =例中，閉鎖料斗係空間地整合至儀磨單元中且以 於至 >、一個細粉狀燃料儲存容器的重力流加以填充。 200946668 4進行本發明之方法，閉鎖料斗系統由兩個或兩個以 上可從外部加壓的閉鎖料斗組成。將閉鎖料斗系統連接至 一上游儲存槽，該儲存槽藉由重力輸送向閉鎖料斗系統供 應細粉狀燃料材料。固體材料之輸送或傳輸受到引入氣體 的有利影響，使得可將影響固體材料輸送或傳輸之氣體引 入裝置女裝於閉鎖料斗系統、密集流輸送管線或饋料槽的 任何適當位置中。 ❿鎖料斗可為任何所需設計。它們可以圓柱體或球體 Z式提供。較佳地’它們具備有一向下排放的錐管，該錐 s之角度由散裝材料之特性決定，用以抵消成拱作用且確 保均均句的材料流。為此原因，在理想狀況下中錐管朝 向底部逐漸變細。燃料材料因此在以重力方向上向下退出 離開。健存槽以及下游饋料槽亦為此種較佳設計。閉鎖料 斗配備有入口閥’經由該等入口閥可對該等閉鎖料斗加 壓。閉鎖料斗裝備有用以控制固體材料流、減壓及加壓或 ^ 進灯壓力補償的現有此項技術之噴嘴、關斷閥閉及控制闕。 在本發明之有利具體實例中，膨脹之氣體可再循環至 碟磨裝置及/或燃料儲存槽。為了在氣體從系統排放或再循 環以供设備使用之前使氣體與粉塵分離，管線較佳繞線經 由粉塵分離器。例如，該等粉塵分離器分離粉塵且將其傳 至適當處置點或將其再循環至儲存槽。理論上有可能在閉 鎖料斗系統、密集流輸送管線、燃料管線或膨脹管線的任 何位置安裝可使氣流與固體材料或粉塵分離之裝置。因 此向閉鎖料斗的氣體側連接處提供饋料槽是有優點的。 17 200946668 管線可在任何所需位置設有氣體引入裝置。舉例而 了，此等裝置可為所謂「增壓器（b00ster)」。然而，特別 是很容易結塊、堵塞或成拱之固體材料的排放裝置可包括 可使固體材料鬆散之額外氣體引入裝置。閉鎖料斗亦可在 任何所需位置設有氣體引入裝置。In the case of the body, it is also possible to use three or more locking hoppers. This is especially recommended in the case of the same equipment output. It is possible to use a plurality of locking hoppers and a plurality of - Zhaohua components. : Two: The facility of the present invention can be any number of locked hoppers and one Zhao =. The number of lock hoppers is determined by the equipment output. - Zhaohua component number = the number of lock hoppers and the number of continuous supply lines. Theoretically any different arrangement is possible. Basically, it is also necessary to use H# and -駚儿_w J Youwan to lock the materials "°, and connect with each other. Any number of connections can be used for this. The preferred connection device is a pipeline. It may also be, for example, a hose or flange 12 200946668 It is also possible to select the interconnection mode of the space as desired. After the tank is twisted, the contained fuel material is discharged in the amount of the ingredients, and then the pressure in the tank is expanded. In the advantageous example of the invention, the inflation gas is used to partially add to the next lock hopper in the cycle. In order to improve the efficacy, this can be carried out by straightening the inflated gas into the tank of the I. In order to reduce the dust load of the expanding gas, the expanding gas is advantageously introduced into a helium dust separator, which is also used to dedust the gas from the storage tank or from the obstruction process. In principle, it is also possible to remove solid material dust from the gas by means of several independent dust separators. To maintain low investment costs, it is advantageous to use only one dust separator. The material flow from the lock hopper is sent to the feed trough via at least one integrated component and a continuous supply line. To take advantage of the present invention, the lock hopper is successively emptied in such a manner that the feed chute is a nearly continuous flow of fuel material. In this manner, a subsequent feed trough of the gasification reactor can be supplied with a continuous stream of material having a pressure suitable for the gasification reaction, wherein the feed level of the feed trough remains almost odd. The level of the filler material of the fuel material in the feed trough can be adjusted according to an advantageous embodiment of the method such that it does not vary by more than ± 30% over a given period of time. If the method of the present invention is carried out by a professional, it is possible to easily maintain the level of the filler of the feed trough within a range of not more than ± 〇 0 〇 / 在 over a period of time. The continuous supply of finely pulverized fuel material from the lock hopper can also be controlled by adjusting the pressure differential between the lock hopper and the feed chute to maintain a constant level of packing material in the feed chute. Gas entering the free space of the lock hopper 13 200946668 σ or exit will affect the pressure difference between the lock hopper and the feed chute and be used as a control parameter for the transport of the solid material. For carrying out the process, the finely divided fuel material preferably has a particle size of less than 0.5 mm. This is achieved by milling and grinding. It is possible to facilitate the discharge of the solid material from the lock hopper by adding a gas to the lock hopper immediately adjacent to the discharge nozzle." By adding gas to the continuous supply line or to the integrated element or both, it is possible to adjust Continuous supply of pipelines to achieve density. At this point, the addition of gas can also be used to purify the continuous supply line or the integrated element. It can also supply the gas to the connecting element between the lock hopper and the integrated component. In an advantageous embodiment of the invention, the 2 gas supply system is recovered in the feed trough and is returned to the lock hopper by means of an injection (4). The return of the delivery gas and the injector are collectively used as a replacement gas for the venting lock hopper to also maintain the lock hopper pressure during the transfer process. In order to meet the requirements of a certain fire, the solid material; the time (four), two or more locks between the lock hoppers are discharged into the transfer line. It can be balanced by Qi Zhao. The method of the present invention, which is advantageously connected to the feed line, can also be used to extend the method. The method steps required after the coal gasification process of the present invention. These 2 routine steps including the reactor can also be used for supplies such as the second (:) cleaning step. It is also possible to measure the stepping, flow rate, force or temperature of the supporting method of the gas that is connected to the loose packing. In particular, the invention also describes an arrangement for carrying out the method. The facility of the present invention may comprise all of the equipment units required to operate a coal gasification plant in accordance with the method of the present invention. The technical solution is also directed to a facility for supplying a solid fuel material to a reactor for gasification of a solid fuel material, comprising: a grinding device, a dust separator, a storage tank, at least two lock hoppers, At least one connecting device for dense flow conveying, a feed trough, a gasification reactor, wherein: the obstruction device is connected to a storage container by means of a connecting device, and the dust separator is mounted to the obstruction device Between the storage tanks, and the storage container is connected to the lock hoppers via connecting means adapted for gravity flow or dense flow transport, and the lock hoppers are suitable for dense flow transport by means of a common use The connecting means of the continuous supply line is connected to a feed chute, and the feed chute is connected to the gasification reactor via other fuel material lines. Dense flow transport from the lock hopper system to the feed trough allows the feed trough to be installed at the same or different geodesic height as the lock hopper system. In the case of the currently known gravity lock hopper system, it is indispensable to mount the lock hopper above the feed chute. With this measure, it is possible to reduce the construction height of the overall equipment 15 200946668 to a considerable extent. It is also possible to position the lock hopper system and the feed trough and reactor in separate buildings. The invention also relates to the advantage of being able to select a lower construction height for each unit. Various device components can be arranged as needed, so that the spatial layout of the device can be flexibly performed. 0 The transfer of fuel material from the lock hopper to the feed trough is via at least one connecting device and at least one body-forming element. The transfer of components to the feed trough is carried out via separate continuous supply lines for dense flow transport. The transfer of the self-locking hopper to the feed trough can be carried out via other integrated components with transfer connections. Depending on the specific example of the method, the fuel material is pressurized using two or more lock hoppers. This is especially true if the material with high fuel material handling capacity or the lock hopper system is to be added to higher pressures. The inlet side of the lock hopper is connected to a feed trough, which feeds the fuel material to the lock hopper by means of both dense flow transport and gravity transport: for this purpose, a suitable between the storage tank and the lock hopper Location safety: a star feeder or a material manifold. It is also possible to install an intermediate container, a spherical container or a gas feedthrough between the storage tank and the lock 枓+. The fuel material supply system may also include any desired disc grinding device or grinder. The grinder can then also include other grinding devices, such as shredders for wood or coal shredders. It is also possible to cover the gas or to use it as an inert gas. [In the comparative example of the present invention, the locking hopper is spatially integrated into the instrument grinding unit and is used to >, a fine powder fuel storage container. Gravity flow is filled. 200946668 4 In accordance with the method of the present invention, the lock hopper system consists of two or more lock hoppers that can be externally pressurized. The lock hopper system is coupled to an upstream storage tank that supplies fine powdered fuel material to the lock hopper system by gravity. The transport or transport of the solid material is advantageously influenced by the introduction of the gas such that the gas that affects the transport or transport of the solid material can be introduced into the device in any suitable location in the lock hopper system, the dense flow transfer line or the feed trough. The shackle hopper can be designed for any desired purpose. They can be supplied in a cylinder or sphere Z. Preferably, they are provided with a downwardly directed cone which is angled by the characteristics of the bulk material to counteract the arching action and to ensure uniform flow of material. For this reason, the cone is tapered toward the bottom under ideal conditions. The fuel material thus exits downwards in the direction of gravity. The storage tank and the downstream feed trough are also such a preferred design. The lock hopper is equipped with an inlet valve' via which the lock hoppers can be pressurized. The lock hopper is equipped with nozzles, shut-off valves and control ports of the prior art which are useful for controlling the flow of solid materials, depressurization and pressurization or compensation of the pressure of the lamps. In an advantageous embodiment of the invention, the expanded gas may be recycled to the disc grinding device and/or the fuel storage tank. In order to separate the gas from the dust before it is vented or recirculated from the system for use by the equipment, the line is preferably wound through a dust separator. For example, the dust separator separates the dust and passes it to a suitable disposal point or recycles it to a storage tank. It is theoretically possible to install a device that separates the gas stream from the solid material or dust at any point in the lock hopper system, the dense flow transfer line, the fuel line or the expansion line. It is therefore advantageous to provide a feed chute to the gas side connection of the lock hopper. 17 200946668 The pipeline can be equipped with a gas introduction device at any desired location. For example, such devices may be so-called "b00sters". However, in particular, the discharge means of the solid material which is easily agglomerated, clogged or arched may include an additional gas introduction means for loosening the solid material. The lock hopper can also be provided with a gas introduction device at any desired location.
在這種狀況下，閉鎖料斗之材料排放處配備有一連接 兀件’來自閉鎖料斗之材料流經由該連接元件傳至一體化 疋件。由於燃料在自閉鎖料斗至饋料槽的整個輸送過程中 處於高於氣化反應器壓力之麼力位準下，目此此等元件應 針對高壓設計。為確保材料流受到控制，有利地是安裝閉 鎖料斗使得它m目對於-體化元件對稱排列，使得閉鎖料 斗與一體化元件之間的連接元件較佳具有相同長度。 一體化元件可為任何所需類型。較佳地，此等一體 元件為呈現混合型元件功能之裝置。此等一體化裝置可 (例如）歧管或γ形歧管，但亦可為所謂「管集箱（叫In this case, the material discharge of the lock hopper is provided with a connecting member. The flow of material from the lock hopper is transmitted to the integrated member via the connecting member. Since the fuel is at a higher pressure than the gasification reactor pressure throughout the entire process of the self-closing lock hopper to the feed chute, such components should be designed for high pressure. To ensure that the material flow is controlled, it is advantageous to mount the lock hopper such that it is symmetrically aligned with respect to the body element such that the connection elements between the lock hopper and the integrated element preferably have the same length. The integrated components can be of any desired type. Preferably, such integral components are devices that exhibit the functionality of a hybrid component. Such integrated devices may, for example, be manifolds or gamma-shaped manifolds, but may also be so-called "tube headers"
header)」。EP 340 419 B1中提供合適一體化元件之實例 此處所述之元件功能相反且用作一體化元件。連接裝置 可為任何所需類型。較佳所用連接裝置為管。亦可能為 管或凸緣。 亦可有利地向連接裝置 散之氣體。若提供複數個一 供應氣體。為此目的，一艘 置。在本發明之具鱧實例中 或氣體引入裝置》 或一體化元件供應用於材料分 體化元件’則它們可分別地被 化元件較佳地設有氣體引入裝 ，饋料槽亦設有氣體注入裝置 18 200946668 在本發明之具體實例中，向饋料槽供應固體材料之管 線通常在固體材料填料水平面上方結束，且視散裝材料之 特性而定，該管線亦可在固體材料水平面下方進入饋料 槽。由於若方法有利地進行，則固體材料水平面僅經受略 微變化’因此此管線可在饋料槽之較低或中央高度位置 處。若固體材料顯示良好氣體保持特性，而此係降低輪迸 至燃燒器所需之額外氣體量，則以此方式有可能在饋料槽 ❹ 中達成低容積密度。 本發明之設施可在任何所需位置設有固體燃料供應系 、统操作所需之設備裝備。此裝備可為泵，但亦可為加^或 冷卻裝置。亦包括閥或關斷裝置。理論上，此等裝備可安 裝於任何位置。亦可能整合注入器。此處，可使用（例如) 所明「增壓器」（氣體注入器），但亦可能使用氣體噴射泵。 $後，本發明之設施亦包括氣體及固體材料㈣溫度計或 爪量感應n、壓力感應器、位準計或其他量測裝置。 〇 I自閉鎖料斗及來自饋料槽之密集流輸送的設計類型 允許在低高度處構造整個設備構造。由於輸送與重力益 關，因此設備裝備可安裝於任何所需位置。藉由此系統， 2間需求可降至相當A的程度。若干閉鎖料斗及上游儲存 以及恆定水平面之饋料槽㈣統允許達成經給定時期、 甚至歷時延長之時段燃料至饋料槽的無故障 送。此有助於設備可靠性且確絲定的高產物品質。 【實施方式】 本發明之設施係藉助於兩個圖式更詳細地說明，具體 19 200946668 實例並不限於此等圖式β 圖1展示一煤氣化設備之處理流程，該設備配備有一 根據本發明用於供應燃料材料之設施。燃料材料1被供應 且引入研磨機或合適碾磨裝置2中。接著將細粉狀燃料材 料經由粉塵分離器3及燃料管線3a傳至儲存槽4中而燃 料係在中間被儲存於該儲存槽處。隨後將燃料供應至閉鎖 料斗5 »所呈現之實施例展示閉鎖料斗中之兩者5a、％。閉 鎖料斗5用以藉由供應氣體而對燃料分批加壓。為此目的， 閉鎖料斗5在至填料中之填料引入裝置6，a及氣體引入裝置 © 6’b上方具備氣體引入裝置6a、6b。在閉鎖料斗5之間存在 補償管線7，其在需要之狀況下可打開。用於減壓之膨脹管 線8離開閉鎖料斗5，經由該膨脹管線8，膨脹氣體可完全 或僅部分用於覆蓋碾磨裝置2。然而，膨脹氣體亦可用於以 惰性氣體覆蓋儲存槽4。為將藉助於鼓風機8b再循環的碾 磨裝置2之再循環氣體8c調整至足夠溫度，管線可具備熱 交換器8d或另一種用於供熱之合適裝置。在閉鎖料斗5&、 5b下游，將細粉狀燃料材料經由合適之連接裝置％、9b排 Θ 放且傳至一體化元件10。可經由氣體管線u向一體化元件 ίο供應氣體。接著將細粉狀材料經由連續供應管線12送至 饋料槽13。 在圖1所示之例示性變型中，兩個閉鎖料斗5a、“使 用經由一體化元件10之連續供應管線12。這係藉著以閉鎖 料斗5a、5b將固體材料經由一體化元件1〇交替地饋入密集 流輸送連續供應管線12中之方式而有利地達成。$ 了使從 20 200946668 ·-個閉鎖料斗5a切換至另一個閉鎖料斗5b的間歇時間最小 化及確保幾乎不中斷地輸送固體材料，將閉鎖料斗5a、5b 兩者以時間上重疊之方式耦接至一體化元件1〇為有利的。 在這方面有幫助的是經由幾乎已放空之閉鎖料斗5a與仍填 滿之另一個閉鎖料斗5b之間的補償管線7進行壓力補償。 顯然’亦有可能且有利的是以兩個以上閉鎖料斗5實施所 述程序。若有兩個以上閉鎖料斗5，則亦有可能使用才剛剛 〇 清空且現在應減壓以裝載來自大氣壓儲存槽4之固體材料 的閉鎖料斗5之膨脹氣體，用於對仍處於大氣壓條件下之 閉鎖料斗5部分加壓。連接裝置9a、9b具備兩個閥（圖中 未不），一者接近料斗排放處，一者接近一體化元件1〇。在 閉鎖料斗5已清空至最低水平面且由接近一體化元件1〇之 閥自一體化元件10關斷之後，推薦在第二閥關閉之前由連 接震置9a、9b處之氣體注入9'a、9，b淨化或吹淨。 在理想狀況下，恆定的填料水平面13a在饋料槽13中 〇 T優勢。饋料槽13之壓力可由氣體補償過程以過量氣體21 或饋入氣體22保持恆定。從饋料槽13處，將固體材料經 由燃料管線14a、14b送至具有一或多個燃燒器16a、16b 之煤氣化反應器15。在此狀況下，將用於供應固體燃料之 整個設施定位於獨立的設備單元，碾磨單元建築物17a中。 將煤氣化反應器15及饋料槽13定位於另一建築物，氣體 產生單元建築物17b中。 針對加壓氣體之需求適度増加而獲得已提及之本發明 優點，該等優點尤其涉及裝備條目》、構造高度及因此投 21 200946668 資成本大量降低以及設備可贵祕祕上 J霏性增加。此係由於用於連續 供應管線12中固體材料之密辈* 在果流輸送的部分氣體（其已用 於使固體材料密度降至饋料槽13φ rr>TW ij肀佔優勢之值以下的值） 因其為過量氣趙而不可用作煤氣化反應器15之饋入氣想， 參見圖2。絲額外裝置可用’則此部分有待作為過量氣體 21不加使用而移除。同時，閉鎖料斗5 (其為主動傳遞料 斗）中常常需要該氣體量作為固體材料排放量之置換。因 此其本身建議藉由使來自饋料槽13之過量氣體21 循環氣體20再循環至閉鎖料斗且將其用於部分取代置換所 Q 消耗之氣體而減少對氣體的需求。這可由一鼓風機或另一 用於增加壓力之裝置來實施。由於同時處於高系統壓力下 之饋料槽13與閉鎖料斗5之間有待克服的低壓力差，注入 器18本身尤其視為一氣體喷射泵。另外該泵亦能夠輸送 含粉塵氣體，無需粉塵分離。推進劑氣體用作用於達成置 換目的之加壓氣體’在顯著較高壓力下可使用該加壓氣 體。注入器18之壓力側切換至當前主動閉鎖料斗。在典型 操作條件下’再循環氣鱧部分佔置換氣體量約25%。同時，〇 推進劑氣體23之供應壓力比閉鎖料斗壓力高約1〇巴，而 再循環氣體20之壓力僅比閉鎖料斗壓力高約丨_2巴。此等 數值關係使得對於專業人員來說，注入器系統18在指定條 件下完全可操作是顯而易見的。 用以下方式將氣體再循環整合至饋料槽13之壓力控制 系統中：基於過量氣體21是要在恆定操作條件下從饋料槽 13移除的考慮，藉由使注入器18吸出所釋放量之氣體且將 22 200946668 中來避免饋料槽13中壓力增加。若饋料 的形式力二繼=’：過多壓力量係以過量氣體21 的話，則此氣體亦可有益地用於 尤取代在各種位置饋入氣化反應器中之淨化氣體。 環氣體2。及過量氣體21之管線中之閱是關閉 月/的啟動程序期間’萬一饋料槽13需要不可能由過 虱體21達成的壓力增加，不足量由新鮮饋入氣體補 償0Header)". Examples of suitable integrated components are provided in EP 340 419 B1 The elements described herein function inversely and serve as an integrated component. The connection device can be of any desired type. Preferably, the connecting means used is a tube. It can also be a tube or a flange. It is also advantageous to disperse the gas to the connecting device. If a plurality of supply gases are provided. For this purpose, a ship. In the case of the invention or the gas introduction device or the integrated component is supplied for the material splitting element', they may be separately provided with a gas introduction device, and the feed channel is also provided with a gas. Injection device 18 200946668 In a specific embodiment of the invention, the line supplying the solid material to the feed trough generally ends above the level of the solid material packing, and depending on the characteristics of the bulk material, the line can also enter the feed below the solid material level Feed trough. Since the solid material level undergoes only a slight change if the method is advantageously carried out, the line can therefore be at a lower or central height position of the feed trough. If the solid material exhibits good gas retention characteristics which reduce the amount of additional gas required for the rim to the burner, it is possible in this way to achieve a low bulk density in the feed trough 。. The facility of the present invention can be provided with a solid fuel supply system, equipment and equipment required for operation at any desired location. This equipment can be a pump, but it can also be a heating or cooling device. Also included are valves or shut-off devices. In theory, these equipment can be installed in any position. It is also possible to integrate the injector. Here, for example, the "supercharger" (gas injector) can be used, but it is also possible to use a gas jet pump. After $, the facility of the present invention also includes gas and solid materials (iv) thermometer or claw sensing n, pressure sensor, level gauge or other measuring device. 〇 I Self-locking hopper and design type for dense flow transport from the feed chute Allows the construction of the entire plant at low heights. Thanks to the transport and gravity benefits, the equipment can be installed in any desired location. With this system, the two requirements can be reduced to a level equivalent to A. A number of lock hoppers and upstream storage and constant level feed troughs (4) allow for trouble-free delivery of fuel to the feed trough over a given period of time, even over a period of time. This contributes to the reliability of the equipment and the high product quality that is determined. [Embodiment] The facility of the present invention is explained in more detail by means of two drawings, specifically 19 200946668 The example is not limited to such a pattern β. FIG. 1 shows a processing flow of a coal gasification apparatus equipped with a device according to the present invention. A facility for supplying fuel materials. Fuel material 1 is supplied and introduced into a grinder or suitable milling device 2. The finely divided fuel material is then transferred to the storage tank 4 via the dust separator 3 and the fuel line 3a, and the fuel is stored in the storage tank in the middle. The embodiment presented with the subsequent supply of fuel to the lock hopper 5» shows both 5a, % of the lock hopper. The lock hopper 5 is used to batch pressurize the fuel by supplying a gas. For this purpose, the lock hopper 5 is provided with gas introduction means 6a, 6b above the filler introduction means 6, a to the filler and the gas introduction means © 6'b. There is a compensation line 7 between the lock hoppers 5 which can be opened if needed. The expansion line 8 for decompression leaves the lock hopper 5, via which the expansion gas can be used completely or only partially to cover the grinding device 2. However, the expanding gas can also be used to cover the storage tank 4 with an inert gas. In order to adjust the recirculating gas 8c of the grinding device 2, which is recirculated by means of the blower 8b, to a sufficient temperature, the line may be provided with a heat exchanger 8d or another suitable means for supplying heat. Downstream of the lock hoppers 5&, 5b, the finely divided fuel material is discharged via suitable connecting means %, 9b and passed to the integrated component 10. Gas can be supplied to the integrated component ίο via the gas line u. The finely powdered material is then sent to the feed tank 13 via a continuous supply line 12. In the exemplary variant shown in Figure 1, the two lock hoppers 5a, "using a continuous supply line 12 via the integrated element 10. This is by means of the lock hoppers 5a, 5b alternating the solid material via the integral element 1" It is advantageously achieved by feeding the dense flow into the continuous supply line 12. The minimization of the intermittent time of switching from 20 200946668 to one lock hopper 5a to the other lock hopper 5b and ensuring that the solids are transported almost uninterrupted It is advantageous to couple the locking hoppers 5a, 5b to the integrated component 1 in a time-overlapping manner. It is helpful in this respect to pass through the locking hopper 5a which has almost been emptied and the other which is still filled. The compensation line 7 between the lock hoppers 5b is pressure compensated. Obviously, it is also possible and advantageous to implement the procedure with more than two lock hoppers 5. If there are more than two lock hoppers 5, it is also possible to use them. 〇 〇 且 且 且 且 且 且 且 且 且 且 且 且 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 部分 部分 部分 部分The connecting devices 9a, 9b are provided with two valves (not shown), one close to the hopper discharge, one close to the integrated component 1 〇. The locking hopper 5 has been emptied to the lowest level and is close to the integrated component 1 After the valve 10 is turned off from the integrated component 10, it is recommended to purify or blow off the gas injection 9'a, 9, b at the connection shocks 9a, 9b before the second valve is closed. Under ideal conditions, a constant filler The horizontal plane 13a has an advantage in the feed trough 13. The pressure of the feed trough 13 can be kept constant by the gas compensation process with the excess gas 21 or the feed gas 22. From the feed trough 13, the solid material is passed via the fuel lines 14a, 14b It is sent to a coal gasification reactor 15 having one or more burners 16a, 16b. In this case, the entire facility for supplying solid fuel is positioned in a separate equipment unit, milling unit building 17a. The reactor 15 and the feed trough 13 are positioned in another building, the gas generating unit building 17b. The advantages of the invention have been obtained with a moderate increase in the demand for pressurized gas, which in particular relates to equipment items. , The height of the production and therefore the increase in the cost of 2009, the cost of the equipment and the increase in the cost of the equipment. This is due to the sedition of the solid material used in the continuous supply of pipeline 12 * part of the gas transported in the fruit stream (which has been used The density of the solid material is reduced to a value below the value of the feed trough 13φ rr > TW ij )) because it is an excess gas and cannot be used as a feed gas for the coal gasification reactor 15, see Fig. 2. Silk extra The device can be used 'this part is to be removed as excess gas 21 without use. At the same time, the gas volume is often required as a replacement for solid material emissions in the lock hopper 5, which is the active transfer hopper. Therefore, it is recommended by itself. The excess gas 21 recycle gas 20 from the feed tank 13 is recycled to the lock hopper and used to partially replace the gas consumed by the Q to reduce the need for gas. This can be done by a blower or another device for increasing the pressure. The injector 18 itself is considered in particular as a gas jet pump due to the low pressure difference to be overcome between the feed chute 13 and the lock hopper 5 which are simultaneously at high system pressure. In addition, the pump is also capable of delivering dust-containing gases without the need for dust separation. The propellant gas is used as a pressurized gas for achieving the purpose of replacement. The pressurized gas can be used at significantly higher pressures. The pressure side of the injector 18 is switched to the current active lock hopper. Under typical operating conditions, the recycled gas fraction accounts for about 25% of the amount of replacement gas. At the same time, the supply pressure of the propellant gas 23 is about 1 bar higher than the lock hopper pressure, and the pressure of the recycle gas 20 is only about 丨 2 bar higher than the lock hopper pressure. These numerical relationships make it obvious to the practitioner that the injector system 18 is fully operational under specified conditions. Gas recirculation is integrated into the pressure control system of feed trough 13 in the following manner: based on the excess gas 21 being removed from the feed trough 13 under constant operating conditions, by aspirating the injector 18 The gas will be used in 22 200946668 to avoid an increase in pressure in the feed trough 13. If the form force of the feed is two = ': the excess pressure is the excess gas 21, the gas can also be advantageously used to replace the purge gas fed to the gasification reactor at various locations. Ring gas 2. And the reading of the excess gas 21 in the pipeline is closed during the month/starting procedure. In case the feed trough 13 needs to be increased by the pressure reached by the crucible 21, the shortage is compensated by the fresh feed gas.
:用作注入器18之推進劑氣體23的加壓氣體由閉鎖料 斗5之壓力控制器來補償控制。視節流閥在推進劑氣體管 線中之位置而定，推進劑氣體之量在介於置換所需氣體量 之70%與1〇〇%之間的範圍内。閉鎖料斗壓力之設定值經由 來自饋料槽13之水平面（或自其重量）之級聯（圖中未示） 決定。關於水平面，提供固定的設定值（例如，5〇% )。若 超過此設定值，則閉鎖料斗5與饋料槽13之間由控制器級 聯控制的壓力差值係降低，使得隨後饋入之固體質量流減 少，且若水平面降至設定值以下，則反之控制器係會操作。 圖3至圖8以實施例展示具有各種數目之閉鎖料斗$ 及一體化元件10的配置。此等閉鎖料斗5及一體化元件1〇 係由管線以不同方式連接。 圖3展示本發明包括三個閉鎖料斗5及一個一體化元 件10之設施’其中各閉鎖料斗5係經由連接裝置9而連接 至一體化元件1 〇 ’且一體化元件1 〇係經由連續供應管線 12而連接至饋料槽13。可經由氣體管線11向一體化元件 23 200946668 ίο供應氣體。 圖4展示本發明包括三個閉鎖料斗5及兩個一體化元 件10之設施，其中兩個閉鎖料斗5係經由連接裝置9a、9b 而連接至第 體化元件l〇a’且第·--體化元件l〇a係經 由另一連接裝置而連接至第二一體化元件1〇b，且第三閉鎖 料斗5係經由連接裝置9c而直接連接至第二一體化元件 i〇b，且第二一艎化元件10b係經由連續供應管線12而連 接至饋料槽13。 圖5展示本發明包括四個閉鎖料斗5及三個一體化元 © 件10之設施，其中兩個閉鎖料斗5係各自經由連接裝置 9a-9d而各自連接至一個一體化元件1〇，此等一體化元件 10係經由其他連接元件9e、9f而連接至第三一體化元件 10c，且第三一體化元件10c係經由連續供應管線12而連接 至饋料槽13。 圖6展示本發明包括六個閉鎖料斗5及兩個一體化元 件10之設施，其中二個閉鎖料斗5係各自經由連接裝置9 而各自連接至一個一體化元件10,此等一體化元件10係經 ® 由獨立連續供應管線12a、12b而連接至饋料槽13。 圖7展示本發明包括八個閉鎖料斗5及兩個一體化元 件10之設施，其中四個閉鎖料斗5係各自經由連接裝置 9a、9b而各自連接至一個一體化元件1〇，此等一體化元件 ίο係經由獨立連續供應管線12而連接至饋料槽 圖8展示本發明包括八個閉鎖料斗5及三個一體化元 件10之設施，其中四個閉鎖料斗5係經由連接裝置9而各 24 200946668 自連接至一個一體化元件l〇a、l〇b，此等一體化元件10a、 1 Ob係經由其他連接元件9而連接至第三一體化元件1 〇c， 且第三一體化元件10b係經由連續供應管線12而連接至饋 料槽13。 【圖式簡單說明】 圖1展示一煤氣化設備之處理流程，該設備配備有一 根據本發明用於供應燃料材料之設施。 Ο 圖2顯示出在圖i中煤氣化設備之氣體產生單元的建 築物。 圖3展不本發明包括三個閉鎖料斗5及一個一體化元 件1 0之設施。 圖4展示本發明包括三個閉鎖料斗5及兩個一體化元 件10之設施。 圖5展不本發明包括四個閉鎖料斗5及三個一體化元 件10之設施。 ❹ 圖6展示本發明包 件丨〇之設施。 圖7展示本發明包括 件丨〇之設施。 圖8展示本發明包括 件10之設施。 六個閉鎖料斗5及兩個一體化元 八個閉鎖料斗5及兩個一體化元 八個閉鎖料斗5及三個一體化元 【主要元件符鍊說明】 1 _燃料材料 2 : 碾磨襞置 25 200946668 3 :粉塵分離器 3 a :燃料管線 4 :儲存槽 5、 5a、5b :閉鎖料斗 6、 6a、6b :氣體引入裝置 6'a、6’b :氣體引入裝置 7 :補償管線 8 :膨脹管線 8a :膨脹氣體管線 8b :鼓風機 8c :再循環氣體 8d :熱交換器 9a-9f :連接裝置 9'a、9'b :氣體注入 10、10a-10c : —體化元件 11 :氣體管線 12、12a、12b :連續供應管線 13 :饋料槽 13a :填料水平面 14a、14b :燃料管線 1 5 :煤氣化反應器 16a、16b :燃燒器 17a :碾磨單元建築物 17b:氣體產生單元建築物 26 200946668 1 8 :注入器 19 :氣體 20 :再循環氣體 21 :過量氣體 22 :饋入氣體 23 :推進劑氣體 PC :壓力控制器 Δρ :作為控制參數之壓力 ❹ 〇 27The pressurized gas used as the propellant gas 23 of the injector 18 is compensated by the pressure controller of the lock hopper 5. Depending on the position of the throttle valve in the propellant gas line, the amount of propellant gas is in the range between 70% and 1% of the amount of gas required for replacement. The set value of the lock hopper pressure is determined by a cascade (or not shown) from the horizontal plane of the feed tank 13 (or from its weight). Regarding the horizontal plane, a fixed set value (for example, 5〇%) is provided. If the set value is exceeded, the pressure difference between the lock hopper 5 and the feed trough 13 controlled by the cascade of the controller is reduced, so that the solid mass flow that is subsequently fed is reduced, and if the horizontal plane falls below the set value, Otherwise the controller will operate. 3 through 8 show, by way of example, a configuration having various numbers of latching hoppers $ and integral components 10. These lock hoppers 5 and integral components 1 are connected by pipes in different ways. Figure 3 shows a facility of the invention comprising three lock hoppers 5 and an integrated component 10 wherein each lock hopper 5 is connected to the integrated component 1 〇 via a connecting device 9 and the integrated component 1 is via a continuous supply line 12 is connected to the feed chute 13. Gas can be supplied to the integrated component 23 200946668 ί via the gas line 11 . Figure 4 shows a device of the invention comprising three locking hoppers 5 and two integrated elements 10, wherein the two locking hoppers 5 are connected to the first body element l〇a' via a connecting device 9a, 9b and - The body element l〇a is connected to the second integrated element 1〇b via another connecting device, and the third lock hopper 5 is directly connected to the second integrated element i〇b via the connecting device 9c, And the second enthalpy element 10b is connected to the feed trough 13 via a continuous supply line 12. Figure 5 shows a facility of the present invention comprising four lock hoppers 5 and three integrated components 10, wherein each of the two lock hoppers 5 is each connected to an integral component 1 via a connection device 9a-9d, respectively The integrated component 10 is connected to the third integrated component 10c via other connecting elements 9e, 9f, and the third integrated component 10c is connected to the feed slot 13 via a continuous supply line 12. Figure 6 shows a facility of the present invention comprising six lock hoppers 5 and two integrated components 10, wherein each of the two lock hoppers 5 is each connected to an integrated component 10 via a connecting device 9, such integrated components 10 The vias are connected to the feed trough 13 by separate continuous supply lines 12a, 12b. Figure 7 shows the arrangement of the invention comprising eight locking hoppers 5 and two integrated components 10, wherein each of the four locking hoppers 5 is each connected to an integrated component 1 via a connecting device 9a, 9b, such integration Element ίο is connected to the feed trough via a separate continuous supply line 12. Figure 8 shows a facility comprising eight lock hoppers 5 and three integrated elements 10 of the present invention, wherein four lock hoppers 5 are each connected via a connection device 9 200946668 self-connected to an integrated component 10a, lb, these integrated components 10a, 1 Ob are connected to the third integrated component 1 〇c via other connecting elements 9, and the third integration Element 10b is connected to feed trough 13 via a continuous supply line 12. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 shows a process flow of a coal gasification plant equipped with a facility for supplying fuel materials according to the present invention. Ο Figure 2 shows the building of the gas generating unit of the coal gasification plant in Figure i. Figure 3 shows the invention including three lock hoppers 5 and an integrated component 10 facility. Figure 4 shows a facility of the present invention comprising three latching hoppers 5 and two integrated components 10. Figure 5 shows a facility comprising four lock hoppers 5 and three integrated components 10. Figure 6 shows the facility of the package of the present invention. Figure 7 shows the facility of the present invention including the components. Figure 8 shows the facility of the present invention including the device 10. Six locking hoppers 5 and two integrated yuan eight locking hoppers 5 and two integrated elements eight locking hoppers 5 and three integrated elements [main component chain description] 1 _ fuel material 2: grinding device 25 200946668 3 : Dust separator 3 a : Fuel line 4 : Storage tank 5, 5a, 5b: Locking hopper 6, 6a, 6b: Gas introduction device 6'a, 6'b: Gas introduction device 7: Compensation line 8: Expansion line 8a: expansion gas line 8b: blower 8c: recirculation gas 8d: heat exchanger 9a-9f: connection means 9'a, 9'b: gas injection 10, 10a-10c: - body element 11: gas line 12, 12a, 12b: continuous supply line 13: feed trough 13a: packing level 14a, 14b: fuel line 15: coal gasification reactor 16a, 16b: burner 17a: grinding unit building 17b: gas generating unit building Object 26 200946668 1 8 : Injector 19 : Gas 20 : Recirculating gas 21 : Excess gas 22 : Feed gas 23 : Propellant gas PC : Pressure controller Δρ : Pressure as control parameter ❹ 〇 27