CN101278034B - System for the conversion of coal to a gas of specified composition - Google Patents

Abstract

The present invention provides a coal gasification system with an integrated control subsystem. The system generally comprises, in various combinations, a gasification reactor vessel (or converter) having one or more processing zones and one or more plasma heat sources, a solid residue handling subsystem, a gas quality conditioning subsystem, as well as an integrated control subsystem for managing the overall energetics of the conversion of coal to energy and maintaining all aspects of the gasification processes at an optimal set point The gasification system may also optionally comprise a heat recovery subsystem and/or a product gas regulating subsystem.

Description

Be used for coal is converted into the system of the gas of specific components

Invention field

The present invention relates to coal gasification, relate in particular to the method and apparatus that coal is converted into the gas with special component.

Background of invention

The coal of different stage can be as the main raw material of gasification.This comprises the low level high sulphur coal, and this kind coal is unsuitable for being used in the generator of coal combustion owing to producing the discharge with high sulfur content.Discarded coal particle and coal dust residual behind digging, storage, the washing coal also are useful for gasification.Coal can gasify to produce so-called " synthesis gas " that contains carbon monoxide, hydrogen, carbonic acid gas, gaseous sulphide and particle with oxygen and steam usually.Gasification step usually in about 650 ℃ to 1200 ℃ temperature range, or normal atmosphere, or more generally carrying out to about 100 atmospheric high pressure from about 20.

Several dissimilar coals are arranged, and each all shows different qualities owing to geology is historical.The development rank of coal is called as coal " grade ".Mud coal is the directly vegetable material layer under growth district that coal forms environment.Vegetable material shows very little variation and contains the root of living plant.Brown coal very young on geology (being less than 40,000 years).It can be soft, fibrous and contain large quantity of moisture (usually about 70%) and have low energy content (8-10MJ/kg).Sub-bituminous coal is the coal of a kind of feature in the brown coal characteristic arrives the bituminous coal characteristic range, and mainly is used as the fuel of steam-power generation.Its lower end in described scope can be dull, dark brown to black, soft frangible, to described upper end become clear, pitch black, hard, and be firm relatively.Sub-bituminous coal contains the inherent moisture of 20 to 30 weight percents.The thermal content scope of sub-bituminous coal is from 20 to 28MJ/kg (not having in constant humidity on the basis of mineral substance).Black coal from 65-105 1,000,000 years in the scope in 26,000 ten thousand years.These are harder more glossy, and moisture is less than 3% energy content that also can have up to about 24-28MJ/kg.Hard coal is moisture-free and contain seldom volatile matter in fact, so its burning produces seldom or do not have a cigarette.It can have the energy content up to about 32MJ/kg.

Ha Beier-Bai Shifa (Haber Bosch Process) according to generation in 1917 makes synthesis gas.This method reaction in the primary reaction of carbon (for example coal) and steam generates the basic reforming reaction of hydrogen and carbon monoxide and operates.The hydrogen of synthesis gas/carbon monoxide ratio extensively changes according to the characteristic of institute's coal supply.But, if with steam reformation one mole of methane, will produce the synthesis gas of rich hydrogen, for example three moles of hydrogen and one mole of carbon monoxide, namely the ratio of hydrogen/carbon monoxide is 1/3.The competitive second order reaction that also is called water-gas shift reaction, wherein carbon monoxide and steam reaction form carbonic acid gas and extra hydrogen.This water gas shift reaction is second order reaction, because high temperature and low pressure help primary reaction.

Because coal often contains sulfide, it is a kind of for the method for coal gasification with generation clean air product fuel that people attempt to provide, and wherein said gaseous product fuel was removed sulphur before using, for example in gas turbines for power generation.In addition, can be purified to remove dust and cinder and a lot of other impurity, for example Qi Hua cinder, the alkali etc. of coal from the gas in gasification zone.

Plasma torch technology has been used for gasification of coal.Plasma torch technology obtains substantial progress and obtains the essence development in nineteen sixty generation, simulates at that time by spaceship and enters earth atmosphere again and the very high temperature condition that produces and develop the plasma generator that makes new advances.Different with the burning torch flame, plasma torch can be operated under oxygen free condition.Plasma torch is to produce by the high temperature that the separation of working gas electricity and ionization is formed the plasma arc midline.The plasmatorch that can buy (torch) can be at the application points lasting high temperature of generation time suitably, and model can get to the output rating more than the 6MW from about 100kW.

Plasma body is the high temperature luminous gas, and it is at least part of ionization, and is made of gas atom, gas example and electronics.Plasma body can generate with any gas in such a way.This provides plasma body interior good control to chemical reaction, because described gas can be (for example, hydrogen, methane, ammonium, the carbon monoxide) of neutral (for example argon, helium, neon), reductibility or (for example, oxygen, the carbonic acid gas) of oxidisability.In the dull stage, plasma body is electroneutral.Thermal plasma can form by making gas pass electric arc.By coming resistance and radiation heating to very high temperature in passing the microsecond of described arc, electric arc will heat described gas rapidly.Common plasmatorch is made of the electrode that elongates coaxial positioned centrally in conduit and the described conduit, and described working gas is by described conduit.In the type of above-mentioned arc, across using High Level DC Voltage as the end of the central electrode of anode with as the slit between the outer electrode of negative electrode.The arc that has caused forming the high temperature electromagnetic wave energy that comprises the ionized gas molecule by the electric current of the gas flow in the slit between anode and the negative electrode.Any gas of gas or mixture (comprising air) can pass through described plasmatorch.

Also have many patents to relate to the different technologies of the coal gasification that produces the synthesis gas that uses in the various uses, it comprises U.S. Patent number 4,141,694; 4,181,504; 4,208,191; 4,410,336; 4,472,172; 4,606,799; 5,331,906; 5,486,269 and 6,200,430.

The gas that produces in the coal gasification process is very warm and dirty usually, and needs further to handle to be translated into enabled production.For example, remove particulate matter and sour gas wet scrubber and the gas of dry type filtering system through being usually used in between pneumatolytic stage, producing.Have been found that many gasification systems, it comprises the system that handles the gas that produces in the gasification process process.

Adaptive, the stable reforming system that reaches operate continuously of the integration needs of coal gasification system and advanced fuel battery technology, described system is applicable to the fuel characteristic of various coals.The gasification system of binding plasma technology provides acceptable variety various coal supply, comprises the possibility of high sulfur content coal.Make the minimized while of energy requirement in reaction vessel, by optimizing the geseous fuel component, the mixing of the partial oxidation condition in the reaction vessel is hoped to offer the best to gasify and constructs.

Synthesis gas (Syngas) can be developed for multiple use, such as the energy that with gas reforming is electricity or chemical application form, for example fuel cell or chemical feedstocks.Be used for that synthesis gas is converted into electric equipment and comprise gas turbine and gas blowing engine at present.These equipment designs are for working in very strict characteristic range and normal very responsive for the variation of gas characteristic.Except influencing power operation efficient, the deviation of gas characteristic even can have negative impact to power operation.For example, the variation of gas characteristic can influence the Anticorrosive Character of lubricating oil in the engine, and it can influence discharge, efficient, pinking and combustion stability equally.Work when therefore, these devices that utilize synthesis gas are in gas characteristic is maintained at boundaries for certain full blast.

Provide background information to be used to make Given information to transmit by being relevant to applicant of the present invention.Need not to permit, also do not answer metaphrase, any information formerly constitutes the prior art of the present invention of conflicting.

Summary of the invention

An object of the present invention is to provide the system that coal is converted into specific components gas, it comprises: gasification reactor vessel, described gasification reactor vessel comprise one or more treatment zones, one or more plasma heat source, be used for adjustable coal feed speed with coal add to described gasification reactor vessel one or more coal input units, be used for adjustable treatment additive feed speed with treatment additive add to described gasification reactor vessel one or more treatment additive input units, and be used for the one or more outlets of the described gas of output; The solid residue processing subsystem; Gaseous mass regulon system; Integrated control system, it comprises: be used for to measure a mistake more the multisystem parameter with the system monitoring device that produces data, the calculating device that is used for collecting and analyzing the data that produced by described system monitoring device, therefore and the emission proper signal is arranged in the take-off equipment that system's one or more systematic regulators everywhere change with influence, and wherein said Controlling System is monitored one or more system parameters and transmitted signals to suitable pained setter to influence the variation in the one or more systematic regulators and to produce the gaseous product of specific components.

In an embodiment of the invention, gasification system can also optionally comprise heat recuperation subsystem and/or gaseous product regulation system.

Brief Description Of Drawings

These and other feature of the present invention will be more clear in following detailed description with reference to the accompanying drawings.

Fig. 1 to 4 is synoptic diagram, and the system that is used for coal is converted into the gas of specific components of the various exemplary embodiment according to the present invention is shown.

Fig. 5 to 10 is synoptic diagram of various downstream application that the system of Fig. 1 to 4 is shown.

The schema of Figure 11 is illustrated in the described system of Fig. 1 to 10 and operationally is coupled to monitoring between the integrated system control subsystem on it and the flowing of the information of adjusting.

Figure 12 is the synoptic diagram that the integrated system control subsystem of Figure 11 is shown.

Figure 13 illustrates the system that is sent to Fig. 1 to 10 by the integrated system control subsystem of Figure 11 respectively or receives the exemplary monitoring of signal and the synoptic diagram of adjusting from it.

Figure 14 is synoptic diagram, the integrated system control subsystem of Figure 11 is shown to exemplary monitoring and the adjusting access point of various device, module and the subsystem of the system of Fig. 1 to 10.

Figure 15 and 16 is synoptic diagram, and the exemplary embodiment for the integrated system control subsystem of Figure 11 to 14 that the input of the plasma gasification container of the system of Fig. 1 to 10 is controlled is shown.

Figure 17 to 19 is synoptic diagram, and various stream (entrained flow) the plasma gasification containers of taking that the system with Fig. 1 to 10 together uses are shown.

Figure 20 and 21 illustrates the flow synoptic diagram of plasma gasification container of various liquefaction that the system with Fig. 1 to 10 together uses.

Figure 22 and 23 is synoptic diagram, and the moving-bed stream plasma gasification container that has the grade option that the system with Fig. 1 to 10 together uses is shown.

Figure 24 is the synoptic diagram that the exemplary heat recuperation subsystem that the system with Fig. 1 to 10 together uses is shown.

Figure 25 illustrates the gas of Figure 24 in further detail to the synoptic diagram of gas type heat exchanger.

Figure 26 is the synoptic diagram that the heat recovery steam producer of Figure 24 is shown in further detail.

Figure 27 is the synoptic diagram of describing for the treatment of from the selectivity steam/water processing subsystem of the steam/water output of the heat recovery steam generation systems (Heat Recovery Steam Generation System) of Fig. 1 to 10 (especially Fig. 2).

Figure 28 is that the integrated control subsystem that illustrates optionally with Figure 11 together uses the various data input and output of plasma gasification method simulation, and the synoptic diagram of system parameter optimization and modeling device.

Figure 29 and 30 is synoptic diagram that another exemplary heat recuperation subsystem that the system with Fig. 1 to 10 together uses is shown.

Detailed Description Of The Invention

Unless otherwise defined, the scientific and technical terminology of this paper that is useful on has the common identical meaning of understanding with the general technical staff of the technical field of the invention.

As being used for this paper, term " about " refer to from rating number+/-10% change.It is understood that such change often is included in any given numerical value provided herein, and no matter whether it is mentioned especially.

Be used for purpose of the present invention, term " synthesis gas " or " synthetic gas " refer to the product of gasification process, and except such as other gaseous state compositions such as methane and water, can comprise carbon monoxide, hydrogen and carbonic acid gas.

As being used for this paper, term " raw material " includes but not limited to any level other coal (comprise and be not suitable for the coal rudimentary, high-sulfur that uses in the power generator of coal combustion).

Term " solid residue " meaning is the solid by-product of coal gasification.Above-mentioned solid residue generally includes inorganic, the incombustible material that is present in the carbonaceous material, such as silicon, aluminium, iron and calcium oxide.The example of solid residue comprises charcoal, cinder and slag.

" slag " means non-leachable (non-leachable), nonhazardous, glassy material, and it is made of inorganic, the incombustible material that are present in the carbonaceous material.Under the hot conditions (1300 ℃-1800 ℃), mineral materials is melted.In case quenching or cooling, the slag of fusing forms glassy mass.This material is applicable to many commercial uses.

As being used for this paper, term " exchange of air " refers to use gas according to the present invention to the gas type heat exchanger, and use is from the enthalpy of the hot gaseous product air after with air heating.

Refer now to Fig. 1 to 10, the invention provides the coal gasification system that has integrated control subsystem 200, with reference to using numeral 10, its exemplary embodiment schematically illustrates in Figure 11 to 16 usually.Described system generally includes (various combination) gasification reactor vessels 14 (or transmodulator), described container has one or more treatment zones and one or more plasma heat source (in 15), solid residue processing subsystem 16, gaseous mass regulon system 20, and integrated control subsystem 200, and described subsystem 200 is used for that integral energy that the management coal is converted into energy flows and conversion and all aspects of keeping gasification are in the setting point (illustrative of Figure 11 to 16 is described) of optimization.Gasification system can also comprise heat recuperation subsystem 18 and/or gaseous product regulon system 22 (for example, as the homogenizing chamber 25 in the embodiment of Fig. 1, as the gas compressor 21 in the embodiment of Fig. 1 and 2 and/or as gas storage 23 in the embodiment of Fig. 4 etc.) alternatively.

The various embodiments that have the coal gasification system 10 of integrated control subsystem 200 are converted into coal the gas of specific components.Particularly, system provided by the invention allows coal effectively is converted into the gaseous product of the component with the downstream application of being applicable to.For example, if gaseous product will for generate electricity by burning at gas turbine (being the reference number 24 among Fig. 1 to 7) or the purposes at fuel cell in use (being the reference number 26 in Fig. 4 and 6 to 10), so what be hoped is the product that obtains can be used as fuel in power generator separately.Perhaps, if gaseous product is as raw material (being the option 28 among Fig. 4) in further chemical process, described component will be best to specific synthetic use.

With reference to figures 11 to 16, integrated control subsystem 200 comprises for measuring one or more system parameters (for example, gaseous fraction (%CO, %CO ₂, %H ₂Deng), gas temperature, gas flow rate etc.) and generate the system monitoring device 202 of data from the system parameter values of described measurement, and be used for described data that Collection and analysis produces from system monitoring device 202 and proper signal exported to the calculating device 204 (by the example logic frame 30 among Figure 16,32 and 34 schematic illustrations) of one or more systematic regulators 206 (that is, Figure 15 and 16 exemplary modulation device 206-1,206-2,206-3 and 206-4).Integrated control subsystem 200 management coals are transformed into the energetics of energy and keep the setting point that described method is in optimization, this is by by the one or more system parameters of monitoring device 202 monitoring, and sends signals to adjust according to the needs of keeping the reaction setting point to suitable systematic regulator 206.Use allows to generate the gaseous product with particular flow rate and component according to the control subsystem 200 of each embodiment of system 10.

With reference to Figure 12, integrated control subsystem 200, especially its calculating device 204 generally includes one or more compressors 208, is used for from the one or more monitor input terminuss 210 of the current system parameter values of each monitoring device 202 receptions with for the one or more conditioner outlet ends 212 that system parameter values new or that upgrade are communicated to each setting device 206.Calculating device 204 (for example can also comprise one or more this locality and/or remote storage device 214, ROM, RAM, removable medium, this locality and/or network insertion medium etc.) for storing various system parameter, setting or vote operating restraints predetermined and/or fine setting herein, system monitoring and control software, but service data etc.Optionally, calculating device 204 can also have or directly or by the different pieces of information storage prepare the entrance that leads to plasma gasification method simulated data and/or system parameter optimization and modeling device 216, and its synoptic diagram is provided among Figure 28.In addition, calculating device 204 can also be equipped be used to the administration portal that leads to Controlling System 200 (system upgrade, maintenance, modification are provided, the adaptation of new system module and/or equipment etc.) one or more diagram user interfaces and input peripheral equipment 218, and for the various output peripheral equipments 220 with data and information of same external source (for example, modulator-demodulator unit, network connection, printer etc.) connection.

With reference to figures 11 to 14, control subsystem 200 of the present invention is guaranteed air-flow and the gaseous fraction from reactor vessel 14, spread all over system 10 alternatively, remain in the predefined tolerance zone so that in optimum condition and generate gaseous product and system's by product (coml slag, gas recovery, steam generation etc.), no matter any natural otherness in the component not at the same level of coal or the similar coal source.The many different coal rank extensively known of those skilled in the art for example.Even in single rank, coal is possible present the material with complex that enriches otherness.The identification of control of the present invention aspect also can adjust to compensate above-mentioned otherness.The monitoring gaseous product such as parameters such as temperature, flow velocity and components, and the arc that changes reactant makes within the predetermined tolerance that is defined with the terminal that the gaseous product parameter is remained on according to synthesis gas.

Integrated control subsystem 200 of the present invention provides correction feedback, feed back to monitor flow velocity, temperature and component one or more of gaseous product by this, and coal input speed, oxygen input speed, steam input speed and total electric weight one or more that are fed to plasma heat source are made correction.Described adjusting is that the variation according to flow velocity, temperature and/or the component of the gaseous product of measuring keeps within the acceptable range to guarantee these.Usually, the scope of flow velocity, temperature and/or the component of selection gaseous product is optimized the gas for specific downstream use.

In the embodiment, method of the present invention uses the controllability of plasma heating to drive gasification simultaneously, and guarantees that the air-flow of described process and component keep within the acceptable range, even the component of coal presents natural otherness.In another embodiment, described process allows the total amount of the carbon that time per unit handles to keep constant as far as possible, and utilizes plasma heating to remain in the boundary of described process with the total heat of guaranteeing time per unit and enter and leave reaction vessel 14.Integrated control subsystem 200 can also be constructed to by as any monitoring in solid residue processing subsystem 16, gaseous mass regulon system 20, heat recuperation subsystem 18 and/or the gaseous product regulon system 22 of schematic illustrations among Figure 14 and/or regulate the generation process.

Coal gasification betides in the gasification reactor vessel 14 of the present invention, its various exemplary embodiment graphic extension in Figure 17 to 23.Gasification reactor vessel 14, except one or more treatment zones and one or more plasma heat source 15, also comprise as the device that is used for coal is input to gasification reactor vessel 14 in 36, with as 38 be used for to add device such as one or more treatment additives of steam or oxidant additive etc., described additive is needed as being used for that gasification is remained on optimization setting point.Gaseous product leaves gasification reactor vessel 14 by the one or more output pneumatic outlets as 40.

In the embodiment, the application of plasma heating combines with input such as the treatment additive of steam and/or oxygen, helps to control gaseous fraction.System 10 also utilizes plasma heating to provide and makes gasification and/or fusing by product cinder and be translated into the required heat of glassy product with commercial value.

The different embodiments of coal gasification of the present invention system 10 also provide the device of the solid by-product that is used for the management gasification.Particularly, described invention provides for originating from the solid residue processing subsystem 16 that solid by-product or the residue of coal to the conversion process of energy is converted into vitrified homogeneous substance of low leachable property.The form of the solid by-product of gasification can be charcoal, cinder, slag or its some combinations.

Illustrative, solid residue processing subsystem 16 comprises solid residue surge chamber 42, plasma heating device 44, slag take-off equipment 46 and control device (it is operably connected to the overhead control subsystem 200 of system 10), by these, plasma heating is used to make the solid fusing, mixes and dense silicon-metal (silicometallic) vitreous material of reaction formation chemically, when flowing out described chamber 42, described material cooled is dense, non-leachable property, silicon metal solid slag.Particularly, described invention provides the solid residue surge chamber, and solid residue wherein uses input speed that integrated control subsystem is optimized to control the rate of heating of plasma body and solid residue to melt fully and homogenize promoting to the conversion of slag.

Each embodiment of coal gasification of the present invention system 10 also provides the device that is used for reclaiming from the gaseous product of heat heat.This heat recuperation subsystem 18 (its exemplary embodiment schematically illustrates in Figure 24 to 26,29,30) comprises transfers to one or more gases to the device of air type heat exchanger 48 with the gaseous product of heat, the gaseous product of described heat is used to add warm air or other oxygenant thus, such as oxygen or rich oxygen containing air.Be can optionally be used for providing heat (seeing Figure 24 and 25) to gasification after the heat of described recovery of form with warm air (or other oxygenant), therefore reduce must by one or more plasma heat sources provide to drive the heat of gasification process.The heat of described recovery can also be used to the heating of industry or dwelling house and use.

Optionally, heat recuperation subsystem 18 also comprises the one or more heat recovery steam producers (HRSG) 50 that can produce steam, and described steam can for example be used as the treatment additive (seeing Figure 24 and 26) in the gasification reaction, or drives the steam turbine generating.

In addition, as seen in Figure 29 and 30, heat recuperation subsystem 18 also can comprise from various other system components and method operationally the additional heat of sucking-off heat reclaim subsystem, such as by plasma heat source method of cooling 53, slag cooling and treatment process 55, GQCS method of cooling 61 etc.Heat recovery system 18 also comprises feedback control system, and this feedback control system is operably connected to the overhead control subsystem 200 of system, to optimize transmission ofenergy (for example, seeing Figure 13 and 14) in whole described system 10.

Each embodiment of coal gasification of the present invention system 10 also provides gaseous mass regulon system (GQCS) 20, or other above-mentioned gas quality regulator (its exemplary embodiment is more detailed explanation in Fig. 1) is converted into the output gas of special characteristic with the product with the coal gasification process.Described gaseous product is directly guided to GQCS 20, and gaseous product described herein must have the output gas of the required feature of downstream application through the treatment step of particular order with manufacturing.GQCS 20 comprises the parts of implementing treatment step, and described step can comprise: for example remove particulate matter 54 (for example by baghouse etc.), sour gas (for example, H from synthesis gas ₂ S removal device 56 and the optional HCl removal device that is used for possible small amount of H Cl, for example the HCl washer 57) and/or heavy metal 58, or humidity and the temperature of regulating described gas during by described system when gas.The existence for the treatment of step and order depend on the component of coal and are used for the specific components of the output gas of downstream application.Gaseous mass regulation system 20 can also comprise integrated control subsystem, and this subsystem is operably connected to the total integrated control subsystem 200 of system 10 and handles (for example, seeing Figure 13 and 14) to optimize GQCS.

Each embodiment of coal gasification of the present invention system 10 also optionally provides the device that is used for the adjustments of gas product as 22, described adjusting is the chemical composition homogenizing by making gaseous product and regulate further feature for example, such as the flow of gaseous product, pressure and temperature to meet the downstream needs.This gaseous product regulon system 22 makes the air-flow that limits feature can be continuously and stably be passed to downstream application, such as gas turbine 24 or engine, fuel cells applications 26 etc.

Particularly, gaseous product regulon of the present invention system 22 provides gas homogenize chamber 25 (Fig. 1) or allied equipment (Fig. 1,2 compressor 21, the gas storage 23 of Fig. 4 etc.), the size that described device has is designed to provide is enough to obtain to export homogenize the uniformly gas residence time of gas of component.Other parts of this gaseous product regulation system are designed to satisfy the needs of the gas performance of downstream application.Described gas regulating system 22 can also comprise integrated feedback control system, and the overall integrated control subsystem 200 that this Controlling System is operably connected to system 10 is optimized flow of energy and conversion and the output (for example, seeing Figure 13 and 14) of this processing.

Refer now to Fig. 5 to 10, those skilled in the art can be understood that native system 10 and integrated control subsystem 200, in different embodiments, can be used to have numerous many energy independent and/or the combination downstream application and produce and conversion system.For example, in the exemplary embodiment of Fig. 5, gasification combined cycle (IGCC) system that described system 10--is integrated--by the synthesis gas that both is provided in one or more gas turbines 24, using, what also be provided in one or more steam turbines 52 using passes through one or more HRSG (s) 50, the steam that produces by described synthesis gas and the discharge gas that is associated with gas turbine 24 are cooled off, and can produce output energy (for example).

In the exemplary embodiment of Fig. 6, described system 10 is with integrated gasification combined cycle (IGCC) system and the solid oxygen fuel cell 26S of system combination, and its latter uses the by product that is rich in hydrogen of synthesis gas to make energy (for example).

In the exemplary embodiment of Fig. 7, described system 10 is with integrated gasification combined cycle (IGCC) system and melting carbonate type fuel cell system 26M combination, and its latter (in Fig. 6) uses the by product that is rich in hydrogen of synthesis gas to come generate energy (for example).

In the exemplary embodiment of Fig. 8, described system 10 will be as 52 combinations of the solid oxygen fuel cell 26S of system among Fig. 6 and one or more steam turbine, and described steam turbine 52 encourages by the steam that the heat that is recovered from synthesis gas and fuel cell output by one or more HRSG 50 produces.

In the exemplary embodiment of Fig. 9, water-gas converter 58 is added in the embodiment of Fig. 8 to be provided for the synthesis gas that is rich in hydrogen among the solid oxygen fuel cell 26S of system.

In the exemplary embodiment of Figure 10, the solid oxygen fuel cell 26S of system of Fig. 9 is replaced by melting carbonate type fuel cell system 26M.

As apparent for those skilled in the art, the above exemplary embodiment of system 10 unexpectedly is determinate, owing to skilled person will appreciate that and other such system architecture and combination can be provided and not depart from overall range of the present disclosure and purport.

Integrated control subsystem

As above brief description, native system comprises integrated control subsystem 200.Described control subsystem 200 comprise for measure one or more system parameters with the system monitoring device 202 that produces data, the calculating device 204 that is used for the data that Collection and analysis produces by system monitoring device 202 (for example, the box 30,32,34 of Figure 16), and send proper signal spreads all over the variation in the one or more systematic regulators that described system arranges (that is, Figure 15 and 16 setter 206-1,206-2,206-3 and 206-4) with influence take-off equipment.Integrated control subsystem 200 supervisory system parameters also send a signal to suitable systematic regulator 206 required various operating parameterss and condition are made real-time adjusting according to making a response about the measured parameter gained data in the system 10.In the embodiment, integrated control subsystem 200 provides feedback control system to manage coal and is transformed into the energetics of energy and keeps the reaction set-point, therefore allows gasification process to carry out producing the gas of specific components under optimized reaction conditions.

The integral energy that coal is converted into gas learn to use this gasification system can be determined and realize.Some factors that influence clean total energy (net overall energetics) mensuration are: the component of BTU value and coal, the diversity factor that the specific components of gaseous product, gaseous product allow and input cost are to the ratio of output valve.Reactant (is for example regulated, the power that is used for plasma heat source 15 and/or 44, such as treatment additives such as oxygen and steam 38, the sorbing agent per-cent in the coal) can carry out with evaluate and optimize clean total energy mode mobile and conversion according to design code.

Therefore, control subsystem 200 of the present invention provides the real-time control of all aspects of described method described method to be carried out to guarantee to learn and will send out at management energy when answering the set-point to maintain in certain tolerance with efficient manner.Therefore, real-time controller can be with all aspects of the integrated described method of mode synchronization control.

The component of the gaseous product of autoreaction container 14 and flow control in the future is in the predefine tolerance by the control reaction environment.Temperature is controlled under the barometric point to guarantee to inject coal intersection under stable as far as possible environment of reaction vessel 14.Control subsystem 200 of the present invention provides control to be transported to the device of the amount of coal, steam and oxygen in the reaction vessel 14.

The operating parameters that can be conditioned to keep the reaction setting point comprises the filler speed of coal, treatment additive filler speed, inductor drum blower fan keeping the power of specified pressure, and plasma heat source () setting and power for example ... plasmatorch 15,44.These control aspects will be referred to each parameter and further discuss.

Specifically with reference to Figure 13 and 14, as above concise and to the point discussion, integrated control subsystem 200 can spread all over described system 10 and integrated monitoring by monitoring device 202, various system parameter, and implements that management energy is learned and each aspect of described method is maintained in some tolerance by setting device 206, various modification to parameter.With these parameters that are discussed in detail hereinafter can produce from one of following or more mutually related methods: plasma gasification container 14, solid residue processing subsystem 16, plasma heat source 15 and slag treatment thermal source 44, heat recuperation subsystem 18 (for example, gas is to air type heat exchanger 48 and/or HRSGB 50) reach any other processing element or the module for the treatment of additive input terminus 38, elementary and/or secondary raw material input terminus 36,39 (for example be rich in the additive of carbon), GQCS 20, homogeneous application chamber (25) and the system 10 related with it.

In addition, owing to have the entrance that leads to these parameters, the various this locality and/or the remote storage device 214 that reach by calculating device 204 (for example lead to many system parameter, system operation scope, system monitoring and control software, operational data and optional plasma gasification method simulated datas of being scheduled to and/or finely tuning and/or the optimized entrance of system parameter and modeling device 216, see Figure 28), integrated control subsystem 200 can also further react so that optimization system output with system 10.

The system monitoring device

Use the system monitoring device 202 of control subsystem 200, can be regularly or monitor many operating parameterss continuously to determine whether system 10 operates in optimum set point.In the embodiment of invention, device 202 is set to monitor in real time described parameter, so its instantaneous telltale that provides system 10 whether to operate in the difference of the permission/tolerance of setting point.Can monitored parameter include but not limited to the temperature of the difference in chemical composition, gaseous product flow velocity and temperature, the system 10, system pressure and various plasma heat source 15,44 the different parameters (that is, power and/or position) of relating to.

Described parameter is monitored in real time and the gained data are used to determine, for example whether need in system, (for example to inject, by setting device 206-2) steaminess/oxygen (or other oxygenant) more, the input speed of coal (for example need be conditioned, by setting device 206-1), or temperature or pressure in any parts not in the system need to regulate.

The system monitoring device can be positioned in any parts of heat recuperation subsystem 18, solid residue treatment unit 16 and gaseous product processing subsystem 22 (if above-mentioned subsystem exist) of GQCS 20 as required.

The component of gaseous product

As previously discussed, if gaseous product is designed to use in generating, the product that it is desirable to obtain so can be used as the fuel of power generator.In the case, the efficient that generates energy by the gas with manufacturing is measured optimum energy.

Its main component is carbon monoxide, carbonic acid gas, hydrogen and steam when output gas leaves reaction vessel 14, and small amount of nitrogen.Methane, acetylene and the hydrogen sulfide that also can have less amount.Carbon monoxide in the output gas or the ratio of carbonic acid gas depend on the amount that is transported to the oxygen in the reaction vessel 14.For example, so that when getting rid of carbon and transforming to the stoichiometry of carbonic acid gas, produce carbon monoxide when the flow of control oxygen, and described process operation be main generation carbon monoxide.

By regulating the balance between plasma heating 15, oxygenant and/or the steam treatment additive 38 that for example is applied, the component of synthesis gas product can be optimized for specific end use (gas turbine 24 and/or the fuel cells applications 26 that for example, are used for generating).Because the chemical action that transforms of during gasification, having added oxygenant and/or steam treatment additive to affect, it is desirable to be provided for to monitor the synthesis gas component as the device in the monitoring device 202.For example change the above-mentioned input of reactant by setting device 206, the synthesis gas parameter is maintained in the predetermined tolerance, described tolerance is used definition by the terminal of synthesis gas.

Use can realize the monitoring of gaseous product such as different monitoring devices 202 such as gas monitor and gas meters.Gas monitor can be used to measure hydrogen, carbon monoxide and the carbon dioxide content of synthesis gas, and its numerical value is spendable in each control in step, describes as the example logic frame 30 of Figure 16 and 32 diagrams.Usually after described gas cooling, and described gas experience regulating step is removed the component of measurement gas product behind the particulate matter.

Use method known to those skilled in the art to carry out sampling and analysing to described gaseous product.A kind of method that is used to measure the chemical composition of gaseous product is to analyze by gas-chromatography (GC).The sample point of these analyses can spread all over described system location.In the embodiment, use the component of fourier-transform infrared (FTIR) the analyser measurement gas of measurement gas infrared spectra.

In the embodiment, monitor such as the monitoring device 202 at axial relief outlet 40 places that the gaseous product parameter of temperature, flow velocity and component etc. can be by being positioned at reaction vessel 14.In another embodiment, thief hole can be installed in any position of gaseous product treatment system.As previously discussed, setting device 206 is set to change the reactant work output and maintains by the terminal of gaseous product with the parameter with gaseous product and use and within the predetermined tolerance of definition.

One aspect of the present invention is by the component of measuring output steam and regulates described method accordingly and determine whether the oxygen that is being added during the gasification is too much or very few.In the preferred implementation, analyzer, sensor or other above-mentioned monitoring device 202 detect existence and the concentration of carbonic acid gas or the rich oxygen containing material of other standard in carbon monoxide stream.

Be apparent that other technology can be used to measure whether mainly generate carbon monoxide.In an alternative, can measure carbonic acid gas to the ratio of carbon monoxide.In another alternative, sensor can be set to measure the amount of oxygen and the carbon amount in plasma generator downstream, calculates the ratio of carbon monoxide and carbonic acid gas, makes the technology adjustment afterwards accordingly.In the embodiment, measure CO and H ₂Value and with itself and target value or scope relatively.In another embodiment, measurement gas product heat value and with itself and target value and scope relatively.

The measurement that is these and other above-mentioned gas product component that it will be appreciated by those skilled in the art that, can run through system's 10 given embodiments by above or other above-mentioned monitoring device 202 carries out, described measurement can be used to monitor and regulate ongoing process so that the work output of process and maximizing efficiency by setting device 206, and therefore not should by on the embodiment that provides of illustrative system that list and that describe by accompanying drawing and control subsystem structure limit.

Everywhere temperature in the system

In the embodiment of invention, provide as the device in the monitoring device 202 and monitored the temperature everywhere that spreads all over system 10 location, wherein obtained above-mentioned data on continuous or basis intermittently.Be used for the monitoring device 202 of the temperature of monitoring reaction vessel 14, for example, can be positioned on the outer wall of reaction vessel 14, or be positioned at the refractory materials of top, centre and the bottom of reaction vessel 14.

The monitoring device 202 that is used for monitoring gaseous product temperature can be arranged at the position of the relief outlet 40 of gaseous product, and spreads all over each position (for example, in the GQCS 20) of gaseous product regulation system.A plurality of thermopairs can be used for monitoring reaction vessel 14 critical point temperature on every side.

Employing is used for holding system's (such as heat exchanger or similar techniques) of the enthalpy that is produced by gasification, in 18, and also can be in conjunction with the monitoring device 202 of the temperature of the each point that is used for the monitoring heat recovery system entrance and exit place of cooling fluid (for example).In the embodiment, gas is to air type heat exchanger 48, heat recovery steam producer 50 (HRSG) or the two is all for reclaiming heat from the hot gas that is produced by gasification.In the embodiment that uses heat exchanger, temperature sensor is set measures, for example, the gaseous product temperature in heat exchanger entrance and exit.Temperature sensor can also be set to measure the temperature of the refrigerant after the heating in described heat exchanger.

Can use the observed value of these temperature sensors to guarantee that when gaseous product enters separately heat exchanger its temperature is no more than the ideal operating temperatures of described equipment.For example in one embodiment, if being used for gas is 1050 ℃ to the design temperature of air type heat exchanger 48, flows to temperature sensor on the entrance of heat exchanger 48 at gas and can be used to control coolant air flow velocity by described system and plasma body heat energy in order to keep the suitableeest gaseous product temperature.In addition, the measurement of gaseous product temperature out helps to guarantee the optimal dose at the enthalpy that has reclaimed from gaseous product in all recovery of heat stages.

Be installed in air stream and go up with the temperature sensor of the exchange of air temperature of measuring heating guarantee that described method carries out under certain condition, described condition is guaranteed to handle air and be heated to the temperature that is suitable for using in gasification.In the embodiment, the coolant air temperature out is for example about 625 ℃, therefore the temperature sensor that is installed on the air stream will provide data, described data be used for determining whether tackling by the air velocity of system and plasma gasification container 14 torch power the two or one of (for example make adjusting, setting device 206-4 by Figure 15 and 16) in order to keep the suitableeest gaseous product input temp, described temperature can be used to control the temperature of coolant air successively.

According to an embodiment of invention, the control scheme arranges fixing setting point for the suitableeest coolant air output temperature, for example about 600 ℃, reaches the fixed value that is used for the HRSG gas outlet temperature, for example about 235 ℃.Therefore, according to present embodiment, when reducing the gaseous product flow, become colder at gas to the gaseous product temperature in the exit of air type heat exchanger 48, cause the steam production reduction because described GRSG gas outlet temperature also is set to fixed value.

When reducing, uses in the air-flow by system same concept.According to an embodiment of the invention, it is fixing that the coolant air temperature of outlet keeps, so gas is warmmer to the temperature of the exit gas product of air type heat exchanger 48, therefore produces more steaminess in HRSG 50.But when the air-flow by system reduces, therefore product gas flow will also reduce, so the temperature in of the increase of HRSG 50 will only be temporary transient rising.For example, be approximate 800 ℃ if air-flow reduces to the maximum gasinlet temperature that 50%, HRSG 50 will temporarily see, it is in the limit of temperature of described heat exchanger designs.

In the embodiment of invention, the monitoring device 202 that is used for monitoring temperature is provided by the thermopair of each position that is installed in system 10 as required.After this, can use aforesaid thermometry by the integrated control subsystem 200 as example logic frame 34 graphic extensions among Figure 16.The temperature survey that is other type that it will be appreciated by those skilled in the art that, can run through system's 10 given embodiments by above or other above-mentioned monitoring device 202 carries out, described measurement can be used to monitor and regulate ongoing process so that the work output of process and maximizing efficiency by setting device 206, and therefore not should by on the embodiment that provides of illustrative system that list and that describe by accompanying drawing and control subsystem structure limit.

System pressure

In the embodiment of invention, the pressure that monitoring device 202 is monitored in the reaction vessel 14 and spread all over total system 10 is set, wherein obtains above-mentioned data on continuous or basis intermittently.In another embodiment, these pressure monitoring devices 202 comprise pressure transmitter, such as the sensator that is positioned on the vertical container wall.The pressure data that relates to system 10 is used need to determine whether to regulate (for example, by setting device 206-1 and the 206-4 of Figure 15 and 16) parameter on real-time basis, such as the interpolation speed of plasma heat source or coal by control subsystem 200.

The otherness of vaporized coal amount can cause quick gasification, and the result is the pressure noticeable change in the reaction vessel 14.For example, increase if add the quantity of the coal in the reaction vessel 14, it is very possible that the pressure in the described container 14 sharply increases.In the above-mentioned situation, advantageously therefore monitoring device 202 monitoring continuously pressure provide by setting device 206 parameter (for example, the speed of inductor drum blower fan) have been monitored to reduce the required data of system pressure in real time.

In another embodiment, for example, provide the continuous-reading of the differential pressure that spreads all over total system 10 by many pressure monitoring devices 202.Can monitor by this way across the pressure difference of each separate part problem accurately to take place in the localization process process rapidly.What it will be appreciated by those skilled in the art that is above and other said system pressure monitor and control device, can be undertaken by different embodiments above or that other above-mentioned monitoring device 202 runs through system 10, therefore described ongoing process makes work output and the maximizing efficiency of process, and should not limited by the embodiment that illustrative system listed above and that describe by accompanying drawing and control subsystem structure provide.

Gas flow rate

In the embodiment of invention, provide monitoring device 202 to monitor and spread all over the locational gaseous product flow velocity that system 10 locatees, wherein obtain data at continuous or intermittent basis.

Gas flow rate by the different parts of system can influence the residence time of gas in specific features.If the gas flow rate in the reformation zone by gasification reactor vessel 14 is too fast, may there be time enough to make the gaseous state composition reach balance, this causes the gasification of non-optimum condition.What it will be appreciated by those skilled in the art that is these and other above-mentioned gas flow monitoring and control device, can be undertaken by different embodiments above or that other above-mentioned monitoring device 202 runs through system 10, to monitor and to regulate ongoing process so that the work output of process and maximizing efficiency by setting device 206, by integrated control subsystem, such as the exemplary control subsystem of describing among Figure 11 to 16 200.

Calculating device

Control subsystem 200 comprises the control reaction conditions and manages coal to the chemistry of output gas and the device of kinetic transformation.In addition, operational condition can be measured and keep to control subsystem 200 to keep desirable, the suitableeest or non-gasification reaction conditions.The mensuration of ideal operation condition depends on the integral power of described process, and described kinetics comprises such as the particular group of the component of coal and the gaseous product factor of grading.The component of coal can be uniformly or can fluctuate in certain degree.When the change of component of coal, some system parameter may need continuous or regular adjusting to keep the ideal operation condition by setting device 206.

Integrated control subsystem 200 can comprise many parts, its each can be designed to carry out special duty, the for example control of the position of one or more of the plasma heat source of the control of a kind of flow velocity of additive, gasification system (for example, 18,44) and power output or the control of by-product recovery.Control subsystem 200 can also comprise treatment system 208, as the treatment unit 208 of calculating device 204.

In one embodiment, treatment system 204 can comprise many sub-treatment systems.Each sub-treatment system can be designed as the reaction model that enforcement can be simulated at least one aspect of reforming plasma reaction.Each reaction model can have the input of its oneself model and model output parameter and can be used to the influence for the variation of model input parameter of the change calculations of model output parameter.Each reaction model can be used to carry out evaluation to help the variation of prediction gasification system operational condition before influencing any function unit of system.Noticeable each reaction model that is can only use in the pre-determined range of operational condition, and simulation and forecast has under the described conditions been simulated the process of (truly) reforming plasma system effectively and accurately.

Described treatment system also can be designed to have department pattern or the complete model of the reaction process of gasification system.With the complete model be the department pattern at top may be very complicated and the variation that can be used to the cumulative operational condition of pre-quantitation maybe can be used to enlarge the scope of operational condition, described model is fully accurately or effectively in this encloses.Abstraction level and the integrity of describing reaction process are more high, and the prediction for the treatment of system is more effective.But the increase of the complicacy of complete model can influence for the practicality of prediction to the model of some influence of the operational condition of gasification system.Their validity can be restricted to prediction in short duration influence or little parameter change.

Figure 28 provides the exemplary embodiment of said system model, and it can be used to be used in combination to limit predicting the outcome on different operating parameter and this basis with integrated control subsystem 200, is used as the starting point of the different processes of implementation system 10.In one embodiment, use these and other above-mentioned model to reevaluate on the basis of carrying out and/or to upgrade different system operation scope and/or parameter temporarily or regularly.In the embodiment, NCR HYSYS analog platform is used and is considered to import any combinatorial input chemical composition, thermochemistry feature, water content, filler speed, treatment additive etc.The optional interactive process optimization that described model also can be used to provide different to be considering, for example, the detail of position and coal type, energy recovery maximization, quantity discharged minimize, investment and minimizing costs etc.Finally, according to the selection of selected type, model can provide, for example low cost of different operating feature, achievable treatment capacity, system design feature, gaseous product feature, emissions levels, recoverable energy, recyclable by product and optimization design.

Every kind of reaction model can be monopolized enforcement in any combination of hardware or software and hardware.As a kind of reaction model that illustrates among Figure 28 can use can by as described in any combination for the treatment of system algorithm, formula or the one group of formula handled describe.If reaction model is monopolized enforcement in hardware, it can become the integral part of described treatment system.

Described treatment system and arbitrary seed treatment system can comprise any combination of hardware or software and hardware exclusively.Arbitrary seed treatment system can comprise one or more ratio (P), integration (I) or differential (D) controller, P-controller for example, I-controller, PI-controller, PD-controller, PID-controller etc.The ideal of the combination of the apparent P of being, I and D controller is selected to depend on the reaction process part of gasification system and kinetics and the time of lag of making up the operational condition scope that will control for those skilled in the art, and kinetics and the time of lag of controller combination.

Importance in the design of combined controller can be the microvibration of short transition period and the transit time when initially regulating each controlled variable or control parameter to rated value.Apparent being for those skilled in the art, these combinations can connect (analog hardwired) form with the analogue hardwired and implement, and described form can be monitored the numerical value of controlled variable or control parameter continuously and itself and rated value comparison are made abundant adjusting by setting device 204 and reduced difference between measured value and the rated value to influence each function unit by monitoring device 202.

The described combination that is that also it will be apparent to those skilled in the art can be implemented in the digital hardware software environment of mixing.Additional any sampling, data obtain and the relative influence of digital processing is known for those skilled in the art, and the Combination Control of P, I, D can be implemented in feedforward and feedback control circuit.

Proofread and correct control

The correction of the control parameter of being monitored by suitable monitoring device 202 or the numerical value of controlled variable or feedback control and rated value are relatively.Control signal is determined according to the deviation between two numerical value, and is set to controlling elements in order to reduce deviation.For example, surpass predetermined H when exporting gas ₂: during the ratio of CO, can measure suitable adjusting to one of output variable as the feed back control system in the calculating device 204, such as the amount that increases additive oxygen with H ₂: the ratio of CO returns to rated value.Be sometimes referred to as the annular time (loop time) time of lag that influences the variation of control parameter and controlled variable by the setting device 206 that is fit to.For example regulating, the annular time of power, the pressure in the system and oxygen and the steam flow rate of plasma heat source can add up to 30 to 60 seconds.

In one embodiment, the component of gaseous product is the rated value that contrasts at above-described feedback control circuit, the CO in the gaseous product and H thus ₂The fixed value (and numerical range) of amount be appointment.In another embodiment, rated value is the fixed value (or numerical range) for gaseous product heating numerical value.

Needing directly monitoring or model prediction is that gratifying all controlled variable and control parameter need feedback control.Exist the controlled variable and the control parameter that are suitable for many gasification systems 10 of in the feedback control circuit, using.Feedback line can be in the each side of control subsystem 206 be effectively implemented, its be used for can be directly perceived and control and their control (for putting into practice purpose) do not rely on those controlled variable of other controlled variable or control parameter or control parameter.

Feed forward control

Feed forward control is handled input parameter influences (do not have and detect) controlled variable and control parameter.Gasification system can use feed forward control to many control parameters, and described control parameter is such as the amount of the energy that is provided to one of one or more plasma heat sources (15,44).The torch power output of plasma heat source (15,44) can be controlled with different approaches, for example, by regulating with the pulse regulation electric current of keeping described arc being applied to torch, change distance between electrodes, the electric current of restriction torch or influence component, direction or the position of torch.

The delivery rate of additive for example can be with some controlling elements control in the feedforward approach, and described additive can gaseous state or liquidly modified or be supplied to gasification reactor vessel 14 with powder type, maybe can spray or otherwise inject by nozzle.But effective control of the temperature of additive or pressure may need to monitor the feedback control with closed loop.

The control of fuzzy logic control and other type

The control of fuzzy logic control and other type can be used for feedforward and feedback control circuit equally.The control of these types may depart from classical P, I, D Combination Control substantially on following meaning: how imitation and simulation reforming plasma reaction kinetics change input variable or output parameter to influence particular result with prediction.Fuzzy logic control only needs the fuzzy of reaction kinetics (system dynamics generally speaking) or experience explanation or system operation condition usually.The aspect of the control of fuzzy logic and other type and the consideration item of enforcement are known for those skilled in the art.

The aforementioned embodiments of inventing that is that to be understood is exemplary and can be different on many degree.Above-mentioned difference present or future will not be considered to depart from purport and the scope of invention, and all such modifications are apparent for those skilled in the art: will be included within the scope of following claim.

The gasification reactor vessel together used of system therewith

Refer now to Fig. 1 to 4 and Figure 17 to 23, coal gasification of the present invention system 10 comprises the gasification reactor vessel 14 with one or more treatment zones and one or more plasma heat sources, in 15.Gasification reactor vessel 14 also comprises as the device that is used for coal is transported to reaction vessel in 36, and as 38 in be used for to add device such as one or more treatment additives such as steam or oxygen/oxygenants, described additive is required in optimum set point as keeping the gasification reaction process.

In an embodiment of the invention, one or more plasma heating source 15 helps coal to the conversion process of gas.Especially, combine with the input of steam and/or oxygen treatment additive 38, the use of plasma heat source 15 helps to control gaseous fraction.Plasma heating can be used for also guaranteeing that the waste gas (offgas) by the gasification generation is converted into their component fully, makes these components be restructured as the gaseous product with specific components.Then, described gaseous product leaves described gasification reactor vessel 14 by one or more output pneumatic outlets 40.

Coal gasification (that is, coal is to the conversion fully of synthesis gas) betides in the gasification reactor vessel 14, and can be under high or low temperature, or carries out under high or low pressure.Many reactions occur in coal are converted in the process of synthesis gas product.Because coal gasifies in reaction vessel, the required physics that gasify, chemistry and processing heat can be according to sending out the design of answering device continuously or generation side by side.

With the coal heating, come moisture-free coal to remove any residual moisture whereby in the gasification reactor vessel 14.Pyrolysis takes place owing to the temperature of dry coal raises.In the pyrolytic process, volatile constituent is volatilized, and when coal was converted into charcoal, coal was thermal decomposited to reduce tar, phenols and light volatile hydrocarbon gas.Charcoal comprises the residual solids of being made up of organic and inorganic materials.

Can further heat the charcoal of gained to guarantee the conversion fully of its gaseous component, keep the cinder by product that is converted into slag after a while.In one embodiment, coal gasification occurs under the condition that has controlled oxygen amount, and the amount of contingent burning is minimized.

Drying, volatilization and charcoal provide the intermediate exhaust gas products to the combination product of the step of converting of cinder.This intermediate waste exhaust gases can further be subjected to heating--usually by one or more plasma heat sources and under the condition that the controlled steam amount exists to finish coal to the conversion of synthesis gas.Final step is also referred to as reforming step.

One or more plasma heat sources can be set so that institute responds simultaneously takes place, maybe can be arranged in the reaction vessel so that they take place in succession.In arbitrary structure, owing to comprise plasma heat source in reactor, the temperature of pyrolytic process raises.

Drive gasification reaction by heating, it can fuel and drive the gasification reaction of heat release with reacting by heating chamber or interpolation as the air of reactant by adding electricity or mineral fuel (for example methane), and it provides heat for reaction.Some gasifications are sent out the process of answering and are also used indirect heating, avoid carrying the burning of material in gasifying reactor, and avoid with nitrogen and excessive CO ₂The diluent gas product.

Described gasification reactor vessel 14 can be based on one of many standard reaction devices well known in the prior art.The example of reaction vessel well known in the prior art comprises, but be not limited to, take stream reaction vessel (Figure 17 to 19), moving-bed (moving bed) reactor (Figure 22 and 23, fluidized-bed (fluidized bed) reactor (Figure 20 and 21), with rotary kiln reactor (not shown), all be suitable in its each by as 36 in the coal input unit accept coal.Add coal by one or more entrances, described entrance is set to top condition and is exposed to heating, is used for fully also effectively coal being converted into gaseous product.

In the embodiment, gasification reactor vessel 14 is designed to or operates close under the normal atmosphere.In another embodiment, reaction vessel is operated under pressurized conditions--and gasification reaction carries out under the pressure between 2 to 10atm.In another embodiment, reaction vessel is under high pressure operated--and gasification reaction carries out under up to the pressure of 30atm.

Gasification reactor vessel can have large-scale length over diameter ratio and can be vertically or flatly directed.Gasification reactor vessel will have one or more gas exhausting devices 40, and be used for (for example removing solid residue, charcoal, cinder, slag or its some combinations) device 16, this device normally is arranged on the relief outlet in the somewhere, (for example, primary furnace 42) bottom along described chamber and removes residue can use gravity flowage.In one embodiment, gasification reactor vessel will use the physical transfer device to remove solid residue from container bottom.For example, hot screw (for example parts 60 of Figure 20) can be used for the cinder by product is transferred to slag treatment chamber 42.The device of processing and processing slag is with more detailed description after a while.The noticeable slag that is also can be handled in the identical chamber of generating gasification (Figure 16 to 19), or handles in the chamber of separating, as in the primary furnace 42 of Figure 20.

According to the present invention, with coal be converted into the synthesis gas product in single locellus reaction vessel, take place in steps.

The design of some gasification reactor vessel 14 is such: the reaction process in a step can take place in the process that coal is converted into synthesis gas, namely herein coal is converted into synthesis gas usually occur in steps in the single zone in the container.In such embodiment, the single step reaction process that is of people imagination occurs in the single zone in the reaction vessel 14, and all herein gasification step occur in the same area.In such situation, the gaseous product that leaves gasification reactor vessel 14 will be the synthesis gas product.

The design of other gasification reactor vessel 14 is such: coal to the step of converting of synthesis gas betide in the described chamber more than in one the zone, namely wherein gasification and reforming step are separated from one another and occur in the different zones in the container on certain degree.

The invention an embodiment in, conversion process takes place in two stages, at first be coal to the waste gas stage, follow and arrive synthesis gas (reformation) stage by waste gas.In two such phase process, people imagination be need be in single locellus reaction vessel at least two discontinuity zones (be used for the first area of gasification step and be used for the second area of reforming step).

In the multizone gasification reactor vessel, first or elementary zone be used for adding hot coal with coal drying (if having residual moisture), the volatile constituent of sucking-off coal, and alternatively the gained charcoal is converted into gaseous product and cinder, therefore produce exhaust gas products, and second area is converted into gaseous product for applying plasma heating fully to guarantee waste gas.Two or more different zones are used for coal gasification and waste gas to the conversion of synthesis gas herein, and the gas that leaves the final area of gasification reactor vessel is synthesis gas.

In one embodiment, driving the required heat of coal gasification provides by adding warm air.In such embodiment, gasification reactor vessel 14 comprises for adding the one or more warm air input units that add that warm air adds the gasification zone to.The described warm air input unit that adds comprises the exchange of air entrance.These entrances are arranged in the reaction vessel will add warm air and spread all over reaction vessel and distribute to start and drive coal to the conversion of gaseous product.

Referring to figs. 22 to 23, can think that reaction vessel 14 described herein comprises the multizone container, wherein gasification occurs in the first area 66, and reforming process occurs in the second area 68 of container 14.Illustrative, in the first area, start the required heat of gasification by the plasma heat source 70 in the embodiment of Figure 23, and provided by the replaceable thermal source in the embodiment of Figure 22 (for example, adding warm air etc.).In these two embodiments, the characteristic of using plasma heat source 72 to reform the gas that produces according to specific output gaseous fraction in second area is used for the processing of passing through gas output 40 subsequently.

Now get back to Figure 17 to 23, what it will be appreciated by those skilled in the art that is by mobile one or more plasma heat sources 15, by adding other thermal source etc., diagrammatic container 14 can be operating as list or multizone reaction vessel 14 and not depart from the application's common scope and purport.In addition, the coal gasification system 10 that being of will being understood has the application of integrated control subsystem 200 can implement with any of above or other above-mentioned gasification vessel structure.In fact, by monitoring the one or more direct or indirect process parameter of in the reaction vessel of given type, implementing about gasification and/or reforming process, whether these processes occur in single zone or a plurality of zone in the single chamber reaction vessel, can pass through monitoring device 202, use the control subsystem 200 of native system 10 to monitor and regulate ongoing process by setting device 206 so that process output and maximizing efficiency.

In addition, still with reference to Figure 17 to 23, gasification reactor vessel comprises one or more treatment additive input units 38 alternatively, and this device 38 is set to useful the adding in the gasification reactor vessel such as gases such as oxygen, air, rich oxygen containing air, steam or other gases of gasification.A mouthful agent input unit is added in described processing can comprise air (or oxygen) input aperture, vapor inlet port and/or sorbing agent mouth.These mouths are arranged on and are used in the reaction vessel 14 treatment additive is spread all over container optimization distribution.The interpolation for the treatment of additive will be described in more detail below.

In addition, according to an embodiment of the invention, described gasification reactor vessel wall lining is with refractory materials.Described refractory materials can be a kind of or combination that is suitable for the conventional refractory materials known in the art that uses in the container that is used for the non-pressurised reaction of high temperature (for example, about 1100 ℃ to 1400 ℃ temperature).The example of above-mentioned refractory materials includes, but not limited to high-temperature calcination ceramic (such as aluminum oxide, aluminium nitride, pure aluminium silicate, boron nitride, zirconium phosphate), glass-ceramic, chromium refractory materials and contains the high alumina refractory of aluminium, titanium and/or chromium.

As understood by a person skilled in the art, according to temperature and the corrosion requirement of specific region, the different zones of gasification reactor vessel can be embedded into different refractory materialss.For example, if there is scorification, advantageously use the refractory materials of non-humidity.

What those skilled in the art will be further understood that is, even above explanation provides the type, structure of reaction vessel, to a lot of examples of the material of its use,, the type of other reaction vessel, structure and/or material do not depart from common scope of the present invention and essence but also can using.

The plasma heating device

Refer now to Fig. 1 to 4 and 17 to 23, system of the present invention uses one or more plasma heating devices, in 15, guarantees to transform fully the waste gas that is produced by gasification has specific components with generation gaseous product.Also can be set to coal is heated to drive the beginning of gasification alternatively as the plasma heating device in 15.

In an embodiment of the invention, one or more plasma heat sources 15 will be set to optimize waste gas to the conversion of specific gas product.According to the design of gasification system, for example, whether use a stage or two stage gasification according to described system, select the position of described one or more plasma heat sources.For example, in using an embodiment of two stage gasifications, plasma heat source can be arranged on respect to the position of exhaust gas entrance and point to the direction of exhaust gas entrance.In another embodiment that uses a stage gasification, described one or more plasma heat sources 15 can extend to the center of gasification reactor vessel.With regard to all situations, select the position of plasma heat source according to the requirement of system, and be used for optimizing described waste gas to the conversion of specific gas product.

Under situation about using more than a plasma heat source, the position of thermal source also is selected to guarantee not conflict between two or more thermals source, for example, there is not thermal source to be subjected to direct heat from another, or the electric arc from a plasma heat source to another not.

In addition, select the position of described one or more plasma heat sources to avoid clashing into the reactor vessel wall that has the plasma body plume, therefore avoid forming " hot spot ".

The obtainable plasma heat source of various commerce that can produce suitable high temperature at the application points place lastingly can be used in the described system.Usually, so spendable model of plasma heat source is that output rating is from more than about 100kW to 6MW.Plasma heat source or torch can use a kind of of proper handling gas or combination.The example of proper handling gas includes, but not limited to air, argon gas, helium, neon, hydrogen, methane, ammonium, carbon monoxide, oxygen, nitrogen and carbonic acid gas.In an embodiment of the invention, the operate continuously of plasma heating device in case produce with waste gas be converted into the synthesis gas product required surpass about 900 to about 1100 ℃ temperature.

Aspect this, many optional plasma torch technology are suitable for using in native system.For example, can be used induction coupled plasma torch (ICP) by being of being understood.Being of also being understood uses transferred arc and the non-transferred arc torch (AC and DC) of the electrode materials of suitable selection also can use.Electrode materials can be selected from, but is not limited to, copper and alloy thereof, stainless steel and tungsten.The graphite torch also can use.Suitably within the common skill scope that is chosen in those skilled in the art of plasma heating device.

In one embodiment, plasma heat source 15 is arranged at the position near one or more air/oxygen and/or vapor inlet port 38, and said air/oxygen and/or steam additive are injected in the plasma body discharge-channel of plasma heat source 15.

In another embodiment, plasma heat source 15 is movable, fixing or its any combination.

Process of the present invention uses the controllability of plasma heating to drive conversion process and guarantee that the air-flow of transmodulator and gaseous fraction maintain in the predetermined tighter tolerances.No matter the component in different coals source, or any natural difference in similar coal source, the control of plasma heating also helps effectively to produce gaseous product.

In one embodiment, control subsystem 200 comprises setting device 206, and described setting device is regulated the power of plasma heat source 15 to manage the clean total output of reacting and to keep the suitableeest setting point.No matter the corresponding filler speed of any fluctuation of coal component and steam and air/oxidizer is in order to manage power that reaction kinetics can regulate plasma heat source 15 to keep constant gasification system temperature.

Control subsystem 200 is with respect to the rated output of institute's location parameter control plasma heat source 15, described parameter is such as the speed of coal and treatment additive being added in the gasification reactor vessel 14, and by temperature sensor with spread all over other above-mentioned monitoring device 202 that the critical positions of system 10 arranges and the system temperature of measuring.The rated output of plasma heat source must be enough to compensation, for example the calorific loss in the gasification reactor vessel 14 and be enough to effectively handle the coal that adds.

For example, when reaction vessel 14 temperature were too high, control subsystem 200 can instruct the rated output that the reduces plasma heat source 15 setting device 206-4 of Figure 15 and 16 (for example, by); On the contrary, cross when low when temperature of fusion, control subsystem 200 can instruct increases the rated output of plasma heat source 15.

In an embodiment of invention, control subsystem 200 comprises setting device 206, and the position of described setting device 206 control torches is to guarantee keeping the suitableeest pyroprocessing zone and to induce favourable flow pattern around entire reaction container 14.

One or more plasma heat sources (in 44) are set to alternatively also to guarantee that the processing fully of the solid residue of gasification handles, as discussing after a while.

The coal input unit

Still referring to figs. 1 to 4 and 17 to 23, the present invention includes as input unit 36 be used for add coal the device of gasification reactor vessel 14 to.Input unit 36 is orientated as and is guaranteed coal is positioned over appropriate location in the reaction vessel, is used for being exposed to the gasification thermal source the suitablelyyest.

In one embodiment, input unit 36 also is provided with setting device 206 and is transported to reaction vessel 14 to guarantee coal with the suitableeest speed for regulating filler speed, is used for gasification reaction is maintained the suitableeest setting point.

In one embodiment, control subsystem 200 comprises setting device 206, and described setting device 206 is regulated input speed mobile and conversion with the clean total energy of management reaction of coal.For example, can regulate coal and add the speed of gasification reactor vessel 14 to promote that coal effectively is converted into gaseous product.The speed of adding coal is selected with the total output according to the design specifications management system of system 10, will react setting point simultaneously and maintain in certain tolerance.

Make the selection of input unit 36 according to the requirement of dispersion, working pressure and the coal particle size of filler.Input unit 206 can comprise wimble, strength haulage system, piston system, stamping system, rotary valve system or top gravity filling system.

Can utilize regulation system, the described coal of preparation before coal adds reaction vessel to.For example, coal can be atomized to necessary quick response size is provided.Usually, the particle size of coal should be 0.75 inch or littler.Coal can pass through the preheater filler alternatively, adds to herein and coal is heated before the reaction vessel.The Powdered coal of such preheating can be transported to reaction vessel by the circuit that adds hot coal.

The input unit for the treatment of additive

Still referring to figs. 1 to 4 and Figure 17 to 23, treatment additive can add reaction vessel 14 to alternatively to promote that coal effectively is converted into gaseous product.Select the type for the treatment of additive and quantity very in earnest so that the conversion optimization of coal, keep meeting the quantity discharged of regulate and control authorities simultaneously and limit and running cost is minimized.Steam input has guaranteed that the free oxygen of capacity and hydrogen are so that the decomposition composition of input refuse is converted into the compound of geseous fuel and/or toxicological harmless substantially.The input of air/oxygen thing helps to handle chemical equilibrium so that the carbon maximization is converted into geseous fuel (uncombined carbon of minimum degree) and keeps the suitableeest treatment temp, and expensive relatively plasma arc input heat is minimized.The quantity of two kinds of additives is determined and very strictly is controlled by work output with processed waste gas.Establish the amount of oxygenant injection very carefully to guarantee at utmost to weigh expensive relatively plasma arc input heat, guarantee that simultaneously total process keeps off and the relevant any processing feature of not expecting of burning, and satisfy and be better than the emission standard of local zone simultaneously.

To produce in the embodiment of electric energy as purpose, it is favourable making the gas with high combustion calorific value at those.The manufacturing of high-quality geseous fuel can be finished by the control reaction conditions, for example is added to the amount of the treatment additive of different step in the conversion process by control.

Therefore, gasification reactor vessel 14 can comprise a plurality for the treatment of additives input aperture 38, described input aperture be set to add to gasification useful such as gases such as oxygen, air, rich oxygen containing air, steam or other gases.Treatment additive input unit 38 can comprise air-in and vapor inlet port.These mouthfuls are arranged on the distribution that is used for optimizing the treatment additive that spreads all over reaction vessel 14 in the reaction vessel.Vapor inlet port can be located strategically that steam is guided to and be centered on the pyroprocessing zone, and before described steam leaves reaction vessel it is guided in the gaseous product material.The air/oxidizer input aperture can be positioned to being planned property and cover in the treatment zone to guarantee treatment additive around reaction vessel.

In one embodiment, control subsystem 200 comprises setting device 206, and described setting device 206 conditioned reaction things flow and conversion with the clean total energy of management reaction.For example, treatment additive can add reaction vessel 14 to promote that coal effectively is converted into gaseous product.Select the type for the treatment of additive and quantity with the design specifications management system total output according to system very in earnest, will react setting point simultaneously and maintain in certain tolerance.In another embodiment of invention, control subsystem 200 comprises setting device 206, and the interpolation of described setting device 206 control treatment additives is to keep the suitableeest reaction set-point.In another embodiment of control subsystem 200, setting device 206 is set controls the interpolation of two or more treatment additives to keep the reaction set-point.In another embodiment, setting device 206 is set and controls the interpolation of two or more treatment additives to keep the reaction set-point.

In those embodiments that comprise a stage process, namely gasification and reforming step all occur in the single chamber gasification reactor vessel 14, and advantageously strategy ground is arranged at the additive input aperture in the gasification reactor vessel 14 and around described reaction vessel and to guarantee to add worker's additive is all covered in the treatment zone.In those embodiments that described process took place with two stages, namely gasify and reformation betides in the intrasystem discontinuity zone, advantageously with close certain zone location of some additive port (for example steam-in), reform by plasma torch or other above-mentioned plasma heat source 15 in described zone.

In another embodiment, control subsystem 200 comprises setting device 206, and described setting device 206 is used for according to from the input by the data adjusting additive of the component gained of each monitoring device 202 and calculating device 204 monitoring and analytical gas product--use the component of these data estimation raw materials.Can continuously or basis intermittently obtain the data of gaseous product component, therefore allow on real-time basis setting device 206-1,206-2 and the 206-3 of Figure 15 and 16 (for example by) to making adjusting such as air, steam and the input of additive of being rich in the additive etc. of carbon.Can also obtain the data of the component of gaseous product on basis intermittently.

Control subsystem 200 of the present invention comprises as the device in the setting device 206, described device is used for concentration when some gaseous product does not join system with additive when not being optimum level according to the intended target level, and described target level is monitored by different monitoring device 202.For example, detect at gas sensor under the situation of too much carbonic acid gas, control subsystem 200 can reduce the transmission of oxygenant in the transmodulator with the generation that reduces carbonic acid gas the setting device 206-3 of Figure 15 and 16 illustrated (for example, by).In an embodiment of invention, regulate described process and mainly produce carbon monoxide, rather than carbonic acid gas.In order to accelerate the generation of carbon monoxide in the above-described embodiment, described system will comprise sensor, analyzer or other the above-mentioned monitoring device 202 for the oxygen level of measuring gas output stream.If the correct oxygen amount of steam or air/oxidizer output is used for described gasification, gaseous product will mainly be carbon monoxide.If hypoxia may form a large amount of elemental carbons or carbon black, they will finally stop up the downstream area of reactor vessel apparatus.If the hyperoxia in the system will produce the carbonic acid gas that too much no essence is worth, if the purpose of described process is to make geseous fuel, this will not expect.Carbonic acid gas too much in the described system is made a response, by the proper signal from control subsystem 200, reduce or eliminate the steam that to be injected into or air/oxidizer any setting device 206-2 and/or the 206-3 of Figure 15 and 16 illustrated (for example, by).

What the coal in the gasification reactor vessel 14 was converted into geseous fuel is thermo-negative reaction, needs that namely energy is offered reactant and can enough be restructured as specific geseous fuel product.In an embodiment of invention, the ratio of gasification institute energy requirement is provided by the initial gas product in the reaction vessel 14 or the oxidized portion of coal.

Oxygenant is added reaction vessel 14 formed partial oxidation action condition in the reaction vessel 14.At partial oxidation on, the carbon in the coal be less than the oxygen reaction of finishing the required chemistry amount of whole oxygenizement.Limited because of available oxygen amount, therefore solid carbon is converted into carbon monoxide and amounts of carbon dioxide, thereby the carbon of gas form is provided.

Above-mentioned oxygenizement also discharges heat energy, thereby has reduced the amount that need introduce the energy in the gasification reactor vessel by plasma heating.Successively, the heat energy of this increase has reduced the amount for the electric power of generation special reaction condition in reaction vessel 14 that is consumed by plasma heat source 15.Therefore, at electric power generation equipment (for example, fuel cells applications 206, gas turbine 24 etc.) in be converted into electric power and the electricity of the more vast scale that produces can be provided to user or output as electric power by geseous fuel because plasma heat source 15 need from the electric power in the system that adopts oxygenant to add produce equipment still less.

Therefore, expensive relatively plasma arc input is minimized keeps the suitableeest required treatment temp simultaneously to the conversion maximization of geseous fuel and making to use the oxygenant input to help to make carbon as treatment additive.Determine that very carefully the injection rate of oxygenant is to guarantee to maximize carbon (CO and the CO that removes gas form ₂).Simultaneously, because the gasification of carbon reaction (with the oxygen combination) be heat release and produce a large amount of heats.This is in the minimized while of needs that makes expensive relatively plasma arc input heat, guarantees that total process keeps off and the relevant any processing feature of not expecting of burning.In an embodiment of invention, oxygenant is air.

Even (because the oxidation of some geseous fuel or carbon release heat energy when the partial oxidation condition exists, therefore and available geseous fuel is still less in the electric power generation equipment) geseous fuel that will in reaction vessel, produce still less, offset the possible loss that electric energy produces by the electric consumption that reduces plasma heat source.In an embodiment of invention, control subsystem 200 comprises that the interpolation of regulating treatment additive is with the equipment of keeping the optimal reaction set-point (for example Figure 15 and 16 setting device 206-3,206-3).

In the embodiment of invention, oxidation additive is selected from air, oxygen, rich oxygen containing air, steam and carbonic acid gas.As in those embodiments of oxide treatment additive, carbonic acid gas can reclaim from gaseous product and recirculation in treatment additive stream at carbonic acid gas.

Economic aim according to conversion process is selected suitable oxidation additive.For example, if economic aim is to produce electricity, provide the suitableeest output gaseous fraction with the selective oxidation additive for given energy generation technique.For those systems that adopt gas blowing engine from gaseous product generation energy, the nitrogen of the higher proportion in the component of gaseous product is acceptable.In such system, air will be a kind of acceptable oxidant additive.But for adopting gas turbine 24 energy-producing those systems, gaseous product before use must be through overdraft.In such embodiment, the nitrogen of the higher proportion in the gaseous product will cause increasing the energy dissipation relevant with the pressurized gas product, and described consume part can not be used as generate energy.

Therefore, in some embodiment, advantageously use the oxygenant of the nitrogen that contains low ratio, such as oxygen or rich oxygen containing air.

Desire to make in the maximized embodiment of generation of electric energy of the present invention, the generation of described electric energy is to use the geseous fuel that is produced by described gasification, and the oxygenizement of the geseous fuel that takes place in gasification reactor vessel is minimized.In order to offset any minimizing owing to the generation geseous fuel of partial oxidation action condition, can be with steam as oxidation additive.The steam input is guaranteed free oxygen and the hydrogen of capacity as the use for the treatment of additive, so that the decomposition components of the coal of input is converted into geseous fuel and/or non-toxic compound substantially.

For producing the embodiment of electric energy as purpose, advantageously produce the gas of high combustion calorific value.Steam is well known in the art as treatment additive.Exist under the condition of steam, coal gasification produces the synthesis gas of mainly being made up of hydrogen and carbon monoxide.Those of ordinary skill in the chemical field will be recognized is that hydrogen in the geseous fuel and the relative proportion of carbon monoxide can control by the treatment additive of different amounts is introduced in the transmodulator.

Vapor inlet port can strategically be located, steam imported in the pyroprocessing zone and/or before described steam leaves reaction vessel 14 it to be imported in the gaseous product material.

In one embodiment, also be provided for sorbing agent is added the device of gasification reactor vessel 14.Because coal contains sulfide, sorbing agent (such as particulate state Wingdale or rhombspar) is delivered in the reaction vessel 14 sulphur that discharges when being vaporized with the absorption coal with described coal.Can add described sorbing agent, with the coal pre-mixing, or it can add by special-purpose sorbing agent mouth before it adds in the reaction vessel 14.Can use integrated control subsystem 200, monitor and conditioned reaction container 14 employed sorbing agents by suitable monitoring device 202 and setting device 206.

The solid residue processing subsystem

Still referring to figs. 1 to 4 and 17 to 23, gasification system of the present invention also is provided for controlling the device of the solid by-product of gasification.Particularly, the invention provides for originating from coal and be converted into the solid by-product of process of energy or glassy, the homogeneous substance that residue is converted into low leachable property.

Particularly, the invention provides solid residue processing subsystem 16, wherein optimize solid residue to the conversion of slag by control plasma heating speed and solid residue input speed to promote fusing fully and homogenization.In one embodiment, the solid residue processing subsystem comprises solid residue Control Room 42 (or primary furnace), and it has solid residue entrance, plasma heating device, slag discharge port, one or more entrances and be used for the slag cooling and be cured as the downstream refrigerating unit of its final form alternatively.Integrated control subsystem 200 of the present invention also comprises setting device 206, this setting device 206 is regulated solid residue to effective conversion of slag by the temperature and pressure that the whole solid residue processing subsystem 16 of monitoring device 202 monitoring is provided, and comprises the device of the operating parameters of controlling above-mentioned energy as plasma heat source 44 and solid residue input speed.

Solid residue processing subsystem 16 of the present invention is suitable for handling the solid residue stream from any process that coal is converted into multi-form energy.This solid residue normally particulate state also can be from one or more sources, such as gasification reactor vessel 14 and optional gaseous mass regulon system 20.In all situations, solid residue is heated to solid is converted into the required temperature of glassy homogeneous substance, described material is extremely low leachable property when allowing cooling and solidifying.

Therefore, solid residue processing subsystem 16 guarantees that solid residue brings up to the sufficient temp that makes the fusing of described solid residue and homogenize.Solid residue subsystem 16 also promotes the catching of pollution solid thing (being heavy metal) in the slag, and the formation of the slag product of cleaning, homogenize (with valuable economically potentially).

In order to ensure the processing fully of solid residue, solid residue processing subsystem 16 is designed to provide sufficient residence time in primary furnace 42.In one embodiment, system 16 provides at least 10 minutes residence time.In another embodiment, solid residue processing subsystem 16 provides 1 hour residence time at the most.In another embodiment, solid residue processing subsystem 16 provides 2 hours residence time at the most.

According to the requirement of native system with removed by product type, can adopt charcoal, cinder, slag or its some array configurations solid residue will relief outlet and conveyer be removed from one or more upstream process continuously or off and on as is known to persons skilled in the art by suitably adopting (adapted).In one embodiment, solid residue is pushed into primary furnace 42 by the system of funnel and transportation screw rod.

Solid residue can add in a continuous manner by using rotary screw or auger device.For example, in the embodiment of Figure 20, adopt spiral conveyer 60 that cinder is passed to primary furnace 42.

Alternatively, solid residue can add with discontinuous mode.In an embodiment of invention, the solid residue input unit that is connected to the solid residue surge chamber can be made up of the transportation pressurized head systems.In such embodiment, adopt the length of limit switch control ram strikes, so can control the amount that each bump is transported to the material in the container.

The solid residue input unit also will comprise control device, so can control the input speed of solid residue to guarantee optimum fusing and the homogenization of solid residue material.

In one embodiment, use plasma heat source 44 with the cinder heating and be molten into slag.Temperature for example is in about 1300 ℃ can periodically or continuously discharge from primary furnace 42 to about 1700 ℃ fusing slag, and forms the solid slag material in cooling after this.Such solid slag material can be used for garbage loading embeading to be handled.Alternatively, the slag of fusing can be poured in the container to form ingot bar, brick and tile or resemble construction material.Solid product also can be ground into gathering materials of conventional purposes.

Therefore, solid residue processing subsystem 16 comprises the slag take-off equipment, discharges from primary furnace 42 by the slag of this device fusing.Take-off equipment can comprise slag discharge port 46, and described relief outlet 46 is usually located near the bottom place of chamber 42 or to promote fusing molten slag bath (pool) to flow out described chamber naturally.Can control the speed that the fusing slag flows out primary furnace with many modes that will it will be apparent to those skilled in the art.For example, in one embodiment, can regulate near the position of plasma heating device and the temperature contrast between the outlet position, with the resolidification time of control fusing slag, for example by adjusting the volume that allows in the chamber, to form the solid residue material in pond.

The slag take-off equipment also is suitable for by keeping primary furnace 42 sealings that the requirement of heating is minimized.In one embodiment, take-off equipment comprises that to pour out groove or S-curved.

As previously discussed, also maybe advantageously the plume of one or more plasma heat sources 44 is aimed at be in or around the molten slag bath of slag discharge port 46 with the temperature of keeping the fusing slag and during guaranteeing complete slag sucking-off slag discharge port remain and open.This practice also help to keep as far as possible slag homogenize prevent that some materials of not handling fully from may inadvertently leave the possibility of solid slag processing subsystem 16 in slag sucking-off process.

Can melt slag from the sucking-off of solid slag processing subsystem with many different methods that those skilled in the art understand.For example, pouring in batches or running through when finishing during handling pours into the sucking-off slag during the entire treatment continuously.Slag from any dump method can be poured in the pouring bath, and water herein act as the sealing between outside atmosphere and the gasification system.Slag can also be introduced into wooden handcart (carts) and abandon, pours into the silica sand bed or pour mould into.

The wall lining of primary furnace 42 is with refractory materials, and described material is a kind of or combination that is suitable for the conventional refractory materials known in the art that uses in the chamber that is used for the non pressurized reaction of very high temperature (for example about 1300 ℃ to 1800 ℃ temperature).The example of above-mentioned refractory materials includes, but not limited to the chromium refractory materials and contains the high alumina refractory of aluminium, titanium and/or chromium.According to the chemical composition of described material and the ability of resisting the corrosive property of slag thereof, utilize their high-density (low porosity) microstructure to select suitable material lining primary furnace.Lower temperature or minimizing heavy metal contamination can reduce corrosion speed.Advantageously select to exist the non-moist fire-retardant material of scorification.

The solid residue surge chamber is designed in fusing and homogenizes the efficient heat transfer between plasma gas and solid residue when handling solid residue.Therefore, when design solid residue surge chamber, consider factors such as the flow such as effectively heat passage, enough Heating temperatures, residence time, fusing slag, the volume of importing solid residue and component.

As previously discussed, the physical Design feature of solid residue surge chamber depends on many factors.These factors comprise, for example, and with component and the volume of processed solid residue.Can collect the solid residue that enters described chamber simultaneously by the source more than.Therefore, the internal structure of solid residue surge chamber and size are stipulated by the operating characteristics of pending input solid residue.

Another factor that will be considered in the design of solid residue surge chamber is to guarantee that solid residue is raised to the required residence time of sufficiently high temperature that makes described solid residue fusing and homogenize.

The type of used plasma heating unit, and the position of described plasma heating unit and direction are another factors to be considered in the design of solid residue surge chamber.The plasma heating device must satisfy and allows the solid residue of gained fusing to flow out described chamber when solid residue being heated to the desired level that makes the fusing of described solid residue and homogenize temperature required.

Control subsystem 200 of the present invention is regulated solid residue to effective conversion of slag by the pressure that monitoring device 202 monitoring temperatures is provided and spreads all over the position of solid residue treatment system 16 alternatively, wherein continuously or basis intermittently obtain above-mentioned data.The monitoring device 202 that is used for the temperature of the described chamber of monitoring for example, can be positioned on the outer wall of described chamber or the inside of the fire-retardant material of top, centre and the bottom of described chamber.Control subsystem 200 of the present invention also provides setting device 206 to be used for the red-tape operati parameter, such as energy and the solid residue input speed of plasma heat source 44.

For example, when temperature of fusion was too high, control subsystem 200 can instruct the rated output that reduces plasma heat source 44; On the contrary, when temperature of fusion is crossed when low, control subsystem 200 can instruct the rated output of rising plasma heat source 44.

In one embodiment, solid residue processing subsystem 16 can comprise that also they can reduce the amount that used heat produces for the device that reclaims heat (for example, Figure 29,30 plasma heat source refrigerating unit 53 and slag refrigerating unit 55).For example, above-mentioned heat reclaim unit can comprise heat exchanger.In a such embodiment, Controlling System can also be controlled the operational condition of heat exchanger.Described heat exchanger for example, can have many temperature sensors, flow control component and other above-mentioned monitoring and setting device 202,206.

Described primary furnace can comprise that also one or more mouthfuls can be inessential additional structural elements/device to regulate.For example, can comprise that a plurality of closed-circuit television mouths keep the viewport of the complete visibility of operator aspect all for the treatment of processes, described treating processes comprises that monitoring is used to form the slag discharge port 46 of sealing.In another embodiment, primary furnace can comprise the service port that allows scouring/cleaning, maintenance and repair in the inlet chamber.Above-mentioned mouthful is the known sealable hole that also can comprise various size in technical field.

Heat recovery system

Refer now to Fig. 1 to 4,24 to 26,29,30, gasification system 10 of the present invention also provides as the device in 18 and is used for recovery of heat from hot gaseous product.This heat recuperation subsystem 18 comprises hot gaseous product is delivered to one or more gases to the device of air type heat exchanger 48--described hot gaseous product is used for adding warm air.The heat that reclaims (exchange of air with heating is form) can be used for providing heat to gasification afterwards alternatively, as specifying in Figure 24 and 25, thereby reduce the heat that must be provided by one or more plasma heat sources 15 that drives described gasification and need.The heat of described recovery can also be used for the purposes of industry or residence heating.

In another embodiment, described gas is used for the oxygenant that heating such as oxygen or rich oxygen containing air are treated to air type heat exchanger 48, provides heat for described gasification alternatively after the described heat exchanger.

Dissimilar gas can be used for native system to air type heat exchanger 48, it comprises sleeve pipe and tubular heat exchange, the two all is straight, single-pass (single-pass) design, and the heat exchanger of the U-shaped pipe of many logical (multiplepass) design, and plate heat exchanger.Suitably the selection of heat exchanger is those skilled in the art's general knowledge.

Because the input temp of ambient air and the significant difference of thermal synthesis gas, gas preferably has its expansion corrugated tube separately to avoid tracheal rupture to each pipe of air type heat exchanger 48.Owing to the problem that the air admission gaseous mixture produces, there is high risk in breaking of pipe.Therefore single tube is blocked and no longer under the situation along with the rest part expansion of tube bank, the breaking of possible generating pipe.

Minimum for risk potential that pipe leaks is dropped to, system of the present invention also comprises with gas and exports the one or more independent temperature sensor that is associated to the gaseous product of air type heat exchanger 48.These temperature sensors are set to be detected and leaks into the temperature that causes because of burning under the ducted situation of synthesis gas in exchange of air and raise.Detect such temperature rising and will cause closing automatically of inductor drum blower fan, described gas blower makes cooling air pass described heat recovery system.

Described gas is designed to make gaseous product to flow in pipeline but not on the sleeve pipe side to air type heat exchanger 48.In one embodiment, gaseous product is with the design perpendicular flow of " cross property (once through) ", and this makes accumulation that particulate matter may take place and the zone of corrosion drop to minimum.In one embodiment, described processing air is in gas adverse current to the sleeve pipe side of air type heat exchanger 48.

Alternatively, the heat recuperation subsystem also comprises the one or more heat recovery steam producers (in 50) that produce steam, as specifying in Figure 24 and 26, described steam can be as the treatment additive in the gasification reaction driving steam turbine 52, or drive such as rotation treatment equipment such as inductor drum blower fans.Use such as heat recovery steam producer (Fig. 1,3,4) or waste heat boiler heat exchangers 50 such as (Figure 24) will be used for adding hot water to produce steam from the heat of gaseous product.In one embodiment, using the steam that produces from the heat of gaseous product is superheated vapour.

Specifically with reference to Figure 24 to 26, describe according to an embodiment of invention to the air type heat exchanger with as the relation between 50 the heat recovery steam producer as the gas in 48.The processing steam additive that described exchange steam also can be used as gasification is with the free oxygen of guaranteeing capacity and hydrogen and make coal farthest be converted into the synthesis gas product.

The steam that is not used to conversion process or driving rotation treatment equipment can be used to other economic aim, such as producing by the steam turbine in use as 52, or purposes is heated in this locality or it can offer local industrial client for its purpose, or it can be used to improve sucking-off oil from Tar sands.

In one embodiment, heat recovery steam producer (or HRSG) 50 is positioned at gas to the downstream of air type heat exchanger 48.In another embodiment, the HRSG50 that is used among the present invention is sleeve pipe and tubular heat exchange.Described GRSG 50 is designed to synthesis gas by the pipeline perpendicular flow, and water seethes with excitement in the sleeve pipe side.

Described gas will be present in the understanding in the described gaseous product and design at some particulate materials to air type heat exchanger 48 and HRSG 50.The size of particle is usually between 0.5 to 350 micron.In one embodiment, described gaseous product speed herein remains on and makes the minimized while of corrosion for the sufficiently high level of pipeline self cleaning.

If the temperature of emission gases product surpasses predetermined threshold, this may show that pipeline is just beginning to stop up, and this moment, described system should close to safeguard.Heat exchanger is set as required, and the mouth that described heat exchanger has is used for surveying, examination and maintenance, and repairs and/or cleanser conduit.

In an embodiment of the invention, system turns round off and on, namely passes through many startups as required and closes circulation.Therefore, the important equipment that is must be designed to stand repetition thermal expansion and contraction.

In order to make the amount of the enthalpy that can from gaseous product, reclaim, reach the exchange of air of the heating that is produced by described heat recovery system and the amount maximization of steam, the pipeline between the parts is provided with the calorific loss that makes surrounding environment alternatively and drops to minimum device.Calorific loss can be reduced to minimum, for example, by use comprise insulating material as known in the art around the insulation barrier of pipeline, or make the minimized device of duct length by design.

With reference to figure 2 and 27, in the embodiment of native system 10, from various steam turbines 52 (for example, the steam turbine of being operated by the steam of HRSG 50 generations is used to cooling down forming gas (circuit 86), therefore the steam turbine that the steam that is produced by HRSG 50 is operated is used for cooling gas turbine/engine 24 and discharging and the gas (circuit 88) that produces, or its any combination) steam that reclaims is by additional heat exchanger 90 coolings by fillers such as cooling tower pumps.In case leave interchanger 90, the steam/water of cooling pumps by exhaust equipment 92, the soft water that is provided with having suitable chemical preparations is therefrom to remove air and excessive oxygen, and the boiler that returns to exhaust HRSG 50 (circuit 94) after the processing is supplied with water, synthesis gas GRSG 50 (circuit 96) etc.

As mentioned above, this gasification system 10 also comprises integrated control device 202, and this device makes the energy of total system shift optimization, therefore controls the kinetics that coal is transformed into energy.Coal is transformed into the kinetics of energy can use native system optimization, has reduced the required input from the heat of external source of the drying that is used for coal and volatilization step because the enthalpy that reclaims is got back to the recycling of gasification.The enthalpy that reclaims also can be used for making the amount of the required plasma heating of the synthesis gas of finishing extra fine quality to drop to minimum.Therefore, the present invention is effectively gasified coal, and the thermal source that wherein gasifies is alternatively by using the air that heats from the enthalpy of gasification product recovery to replenish.

In order to optimize efficient of the present invention, described integrated control subsystem 200 also is provided for controlling the condition of this process of enforcement and the device of operating according to the operational condition of system of the present invention.These control device that can be attached to total system control device 200 are set to monitor one or more parameters, described parameter comprises, but be not limited to, spread all over temperature and the gas flow rate of the specific position of system, and regulate accordingly that ginseng is made condition in case with system held in the parameter of determining.Can pass through control device, the example of the operational condition of being regulated by setting device 206 comprises the input speed of one or more exchange of air flow velocitys, gaseous product flow velocity, coal, such as the input speed for the treatment of additives such as steam with supply with plasma heat source 15,44 energy etc.

For example, temperature sensor (with other such monitoring device 202) can be installed in the specific position of total system 10.Temperature sensor can be mounted to measure, and for example gas reaches the temperature of the gaseous product at HRSG entrance and exit place to the temperature of the gaseous product at the entrance and exit place of the thermoconverter of air.Temperature sensor can also be configured to measure the temperature of the processing air after gas is heated in the air type heat exchanger 48, and the temperature when measuring steam and leaving HRSG 50.

Temperature survey can be used to guarantee that its temperature is no more than the ideal operating temperatures of this equipment when synthesis gas enters each heat exchanger.For example, if gas is 1050 ℃ to the design temperature of air type heat exchanger 48, the temperature sensor on the inlet air flow of described heat exchanger can be used to control by the flow velocity of the exchange of air of system and plasma body heat energy the two in order to keep the suitableeest synthesis gas temperature.In addition, the measurement of gaseous product temperature out is to guaranteeing that the optimal number that reclaims from the gaseous product enthalpy in two heat recuperation stages is useful.

Be installed in the temperature of the heated exchange of air of temperature sensor measurement on the air stream, described exchange of air guarantees that described process implements guaranteeing to handle under air is heated to the temperature that is suitable for using in gasification the condition.In one embodiment, the outflow temperature of exchange of air is, for example about 600 ℃, therefore be installed in temperature sensor on the air discharging current will be used in Controlling System air velocity and the reforming plasma chamber the plasma heat source power the two or one of in order to keep the suitableeest synthesis gas input temp, it can be used to control the temperature of the exchange of air of heating successively.

According to an embodiment of invention, the control scheme fixedly installs a little for the suitableeest outflow temperature being provided with of the exchange of air of heating, and for example about 600 ℃, and the temperature out fixed value of HRSG gas, for example about 235 ℃.Therefore, according to present embodiment, when the synthesis gas flow reduced, gas turned cold to the Outlet Gas Temperature of air type heat exchanger 48, caused steam production to reduce because the temperature out of HRSG gas also is set to fixed value.

When reducing, uses in the air-flow by system same concept.According to an embodiment of the invention, it is fixing that the exchange of air temperature of outlet keeps, so gas is warmmer to the temperature of the exit gas product of air type heat exchanger 48, therefore produces more steaminess in HRSG 50.But when the air-flow by system reduces, therefore product gas flow will also reduce, so the temperature in of the increase of HRSG 50 will only be temporary transient rising.For example, be approximate 800 ℃ if air-flow reduces to the maximum gasinlet temperature that 50%, HRSG 50 will temporarily see, it is in the limit of temperature of described heat exchanger designs.

In addition, if required of the air ratio gasification that is preheated are used for control and will handle the setting device 206 that air is discharged to the self-acting valve of atmosphere and also be set up alternatively and be attached in the total system control device 200 more.For example, under the certain situation, because the precaution of equipment (for example, starting and bolt down procedure), necessary is to add the required more air of ratio of specific heat process.In such example, excessive exchange of air can be discharged from as required.

Described system also can comprise one or more device for the input speed (seeing Figure 15 and 16) of the input speed of monitoring synthesis gas component, coal and treatment additive in order to more information is provided, as may being that to implement to keep the aligning step of the suitableeest treatment condition required.Various above-mentioned monitoring devices 202 are known in the art and can be used in the system of the present invention.

With reference to Figure 29 and 30, above-described heat recuperation subsystem 18 also can be according to filtration and the required cooling that gaseous product is provided of regulating step subsequently, namely about GQCS 20 (for example, GQCS refrigerating unit 61), and (for example provide plasma heat source 15,44, thermal source refrigerating unit 53), the cooling of slag treatment and treatment unit (for example, the slag refrigerating unit 55) etc.

Gaseous mass regulon system

Refer now to Fig. 1 to 4, coal gasification of the present invention system 10 also provides gaseous mass regulon system (GQCS) 20, or other such air regulating device, and its product with the coal gasification process is converted into the special characteristic of output gas.

Therefore make gaseous product will guarantee that gaseous product does not contain chemistry and particulate contaminants by GQCS 20, and can be used for the energy generation systems or for the manufacture of chemical preparations.Be not in the embodiment of purpose to generate energy or manufacturing chemistry goods at those of invention, this regulating step also can be necessary.For example, adjusting subsystem 20 with gaseous mass handles and keeps strictly observing local emission standard when gaseous products can guarantee to discharge described gaseous product by gas barrier.

In one embodiment, gasification system 10 of the present invention purpose is to make the geseous fuel that is suitable for being transported to the renewable electric energy of gas turbine 24 generations with special characteristic (that is, the calorific value of component, heat production, purity and pressure).Because produce fuel by the pyrolysis/gasification of process described herein by coal, this will exist a certain amount of refuse impurity, particle and/or sour gas, and these are not suitable for the operation of the normal and safety of gas turbine.

Described gaseous product is directly guided to GQCS20, and gaseous product described herein must have the output gas of the required feature of downstream application through the treatment step of particular order with manufacturing.As outlined above, GQCS20 comprises the parts of implementing treatment step, and described step can include, but not limited to remove particulate matter 54, sour gas (for example, H from synthesis gas ₂ S removal device 56 and the optional HCl removal device that is used for possible small amount of H Cl, for example the HCl washer 57) and/or heavy metal 58, or humidity and the temperature of regulating described gas during by described system when gas.The existence of required treatment step and order depend on the component of synthesis gas and are used for the specific components of the output gas of downstream application.As previously discussed, system 10 comprises that also integrated control subsystem 200 is to optimize the GQCS process.

In one embodiment, under the vacuum sucking-off condition of the inductance fan of gasification system, the gaseous product of heat is extracted out from gasification system continuously by the exhaust outlet 40 of gasification system.Gas transfer device such as conduit or other pipeline etc. is used to gas is passed to GQCS 20 from vaporizer 14.

Being of also being thought over can be used one or more GQCS 20, such as main GQCS and time GQCS.In this case, described GQCS can be used to handle from main GQCS, shift out such as materials such as particulate matter and heavy metals.Output gas from GQCS 20 can be stored in the gas storage tank (tank) 23 (Fig. 4), by such as depths such as (Fig. 1), the chamber 25 reason device filler that homogenizes, or directly filler to its downstream application that is designed (that is Fig. 2 and 3).

As previously discussed, advantageously be provided at the above-mentioned regulating step device of cooling hot gas product before.For the damage of sensitive component in the anti-locking system, this cooling step may be necessary.In one embodiment, carrying out cooling step by heat recuperation subsystem 18--the heat that reclaims from gaseous product also is recovered alternatively and recirculation is used at gasification system (seeing Figure 24 to 26).

In another embodiment, from the gas of gasification system at first by being cooled such as the direct moisture evaporation in the vaporizers such as cooling pool (not shown).In another embodiment, wet cooling tower (dry cooling) can be used to cool off the synthesis gas that enters GQCS 20 from gasification system.Wet cooling tower can cooling down forming gas temperature from about 740 ℃ to about 150-200 ℃.This process can use adiabatic saturation method to finish, and described method comprises in a controlled manner directly injects air-flow with water.Described transpiration cooling process is a kind of dry process of cooling, and can be monitored to guarantee that cooling gas is not wet, and namely the relative humidity of cooling gas still is lower than 100% under cooling temperature.

As previously discussed, GQCS 20 can comprise as the device in 54, described device is used for alternatively from cooling gas, and removes particulate matter with the inconsistent gas pollutant of downstream use of gaseous product, and described purposes such as burning in gas turbine 24 is to produce electricity or be used as raw material 28 in further chemical production processes.Add particle removal system 54 to remove the particle that may be entrained in the geseous fuel that leaves transmodulator.Particle removal system 54 extensively can get, and for example can comprise, high temperature (pottery) strainer, cyclone separator, Venturi scrubber, electronic filter, candle filter, cross-stream filter, granular filter, water scrubber, textile bags filter chamber strainer (Fig. 1) etc., these professionals for gas regulation extensively know.

As known in the art, particle can be removed in many ways according to its size.For example, use cyclone separator or strainer can remove coarse particles.Littler or thinner particle can use Wet ESP or baghouse strainer (Fig. 1) to remove.In one embodiment, for reaching 10g/Nm ³Particulate load, need to remove the physical barrier of particle with 99.9% efficient.Wet ESP is driven and may be unsuitable for together using with the air-flow of rich oxygen content by electrostatic field, the control device of the turn-off current when described air-flow does not have as oxygen level arrival specified level.

In one embodiment, first particulate abatement device is used to remove coarse particles, and second particulate abatement device is used to remove littler or thinner particle.In one embodiment, first particulate abatement device is the cyclone strainer, and it can remove size greater than the particle of 5-10 micron.In another embodiment, second particulate abatement device is the baghouse strainer.

Interchangeable embodiment can change the order of gas with various purifying step more effectively to use the feature of interchangeable gas-cleaning installation.But according to the specific particle removal system that adopts, it is desirable to before geseous fuel enters aforesaid particle removal system, will leave the described geseous fuel cooling of reaction vessel 14.If the strainer of bag type is used to particle removal, the cooling of geseous fuel may be particularly important, because the bag type filter is often based on Mierocrystalline cellulose or organic polymer, and can not resist extremely high temperature.

Afterwards, dust is collected and can be sent back to gasification reactor vessel, so makes or produce the solid waste of toxicological harmless in gas regulating system.Or described particle can be directed to slag holder (see figure 1) so that the solid that cleans out (scrubber solid) is glassed to non-leachable slag.In some cases, according to precaution and the local regulations of equipment, can be sent to from the solids of gas treating system and to be used for safe handling outside the factory.

Can also arrange as the device in 58, described device is used for removing mercury or other heavy metal from gaseous product.For example, dried injected system is utilized the activated carbon of calculated amount, and described activated carbon injects air-flow with the residence time of abundance, and so consequently trickle heavy metal particles and gas can be absorbed in the activated carbon surface.The heavy metal that is absorbed on the activated carbon can be collected in the baghouse strainer.Or Wet ESP system can be used for collecting the heavy metal that is absorbed on the activated carbon.In an embodiment of invention, the heavy metal particles that is absorbed on the activated carbon is collected in the baghouse.

The effective technology of heavy metal is collected by the acid elution system.This system need make the passage of the gas that contains heavy metal pass to have the packed column of the solution circulation of low pH (1-2 usually).Heavy metal and heavy metal compound and acid-respons form their stable compound.Use this technology, the heavy metal concentration in the circulation solution will increase and therefore need handle gained waste water.In one embodiment, GQCS 20 comprises the acid elution system of removing heavy metal.

In one embodiment, the mercury sander by activated carbon provides the mercury removal device.The activated carbon filter bed can be used as the final grinding apparatus for heavy metal.Gaseous product is by activated carbon beds, and described bed will absorb heavy metal (mainly being mercury) from air-flow.Normally, activated carbon filter is used to realize that the above mercury of 99.8-99.9% removes, and as the final grinding apparatus of the WC pressure difference that has the 7-8 inch.

Acid is gone recovery system 56 to be incorporated into gas regulating system 20 and is reclaimed sulphur or sulfuric acid (from high sulphur coal) and the hydrochloric acid (from chlorinated hydrocarbon) that may have marketable value.Acid removal system 56 can comprise scrubber system, sour removal system and relate to sulphur and/or other conventional equipment of sour removal system.

Following paragraph will replace with new data to be supplied

The gaseous product that produces in the coal gasification system will comprise such as HCl and H ₂Sour gas such as S.The scope of the concentration of these sour gas in the gaseous product: HCl is from about 0.05 to about 0.5%, and H ₂The scope of S is to about 1000ppm from about 100ppm.In one embodiment, the expectation concentration of HCl is about 0.178%, and H ₂The expectation concentration of S is about 666ppm (0.07%).Quantity discharged restriction for HCl is about 5ppm, and for SO ₂, described restriction is about 21ppm.

Removing sour gas can realize by dry washing and wet scrubbing.The major portion of dry washing is spraying drying resorber and yellow soda ash or the lime powder syringe before baghouse filters.Normal dry washing is difficult to realize surpassing 99% acid removal efficient.

If the amount of chlorine is significant scale economically, described chlorine can be recovered.If chlorine exists with insignificant amount, with any suitable mode with its removal (for example, water or wet cleaner, activated alumina absorption etc.).Gas can be processed to remove the composition such as chlorine in gas/liquid washer-contactor.Best wet scrubbing is the mass transfer of the long-pending and little pressure difference of the large contact surface that transmits of heat, and this will help gas cooling.Sodium hydroxide is the conventional alkaline solution for wet scrubbing.In one embodiment, packed column is used to wash sour gas.

The compound of sulphur at first makes up, or as elementary sulfur, as sulphur-oxygen compound or sulphur-hydrogen compound.In one embodiment, the amount of sulphur compound proof cost is reasonable, is set up in the position near heat exchanger along pipeline as the sulfur recovery unit in 76, and the local sulphur compound that temperature reaches becomes stable.The kind of sulfur recovery unit 76 and model depend on the flow of the expectation in the inlet air flow.

If the sulfur content of expection is very low, as desired in the coal of low-sulfur level, the iron filling technique can be used to make sulphur and elemental iron reaction to generate iron sulphide.This is implemented by circulation shot between ducted chamber and recovery chamber.

For the coal that contains high sulfur content, subordinate phase liquid scrubbing process is used to remove the compound of sulphur from gas.By any suitable technology, according to the amount of the sulphur of the expection in the inlet air flow, can be with removal of sulphur.Further downstream area, the amine washer is removed hydrogen sulfide and sulfurous gas from air-flow, stay the air-flow that mainly contains hydrogen, carbon monoxide and rare gas element.Such amine washer is well known in the art and generally includes the processing of amine, and wherein the aqueous solution of monoethanolamine (monoethanoloamine), diethanolamine (diethanoloamine) or methyldiethanolamine is used to remove H from handle gas ₂S.Other method that reclaims sulphur can comprise, for example, and claus plant (Fig. 1), Resox reduction process, the sepn process of cold plasma hydrogen sulfide etc.

In addition, the proper method of removing sulphur comprises, for example, use the wet absorption of NaOH or triazine, use the dry method of Sufatreat to absorb, such as Thiopaq (a kind of biological desulfurizing technology) biological method of etc.ing, or comprise the selective oxidation method of liquid oxidation reductive agent (hanging down CAT).In one embodiment, use the Thiopaq (see figure 1) with H ₂S removes from synthesis gas.Thiopaq is two-step approach, and wherein with weak caustic solution (pH 8.5 to 9) washing acid gas, and sulphur is recovered (by bioprocess, HS-is oxidized to elementary sulfur) subsequently.Other method can comprise, but be not limited to, moving-bed zinc titanate or ferrite absorption process, the oxidation chemistry reaction process (for example, Stretford and SuLFerox) and Slexol acid removal method, the latter of these methods (for example is usually included in high pressure, 300-1000psi) use physical solvent (for example, Polyethylene glycol dimethyl ether) down.

In addition, even the plasma gasification condition is known as the formation that hinders two chalk English, but exist under the condition of carbon, carbon is as catalyzer, and two chalk English can form under 250-350 ℃ temperature.For minimizing that two chalk English form, cooling down forming gas finishes to guarantee to finish quick cooling usually between the said temperature scope in water cooler or spraying drying resorber in addition.In synthesis gas, inject activated carbon and will absorb two chalk English and furans at carbon surface, in the baghouse strainer, remove subsequently.

Can also be used for removing moisture and/or preventing condensation in conjunction with mist eliminator or reheater.Can also comprise that heat exchanger is to arrive the geseous fuel reheat by the required temperature in of downstream generating set.Comprise alternatively that also compressor is to be compressed to geseous fuel the required inlet pressure of downstream generating set.

In another embodiment, humidity conditioner can be the part of GQCS 20.Humidity conditioner act as the downstream application that the humidity of guaranteeing to export gas is suitable for adopting.For example, humidity conditioner can comprise refrigerating unit with cooling draught and therefore from air-flow condensation go out some moisture.These moisture can be removed by gas/liquid separation.In one embodiment, flow of process air guarantees that the air-flow that leaves GQCS 20 has about 80% humidity under 26 ℃ like this.Can be stored (for example, in gas storage 23) after the described gas.

In another embodiment, the gas processing subsystem can comprise the device that reclaims carbonic acid gas and/or the device that reclaims ammonium.Proper device is known in the art.

Gaseous product is also sampled analyzes to determine chemical composition for gas-chromatography (GC).Processing/pollution that the sample point of these analyses spreads all over gaseous product alleviates subsystem and distributes.

In one embodiment, control subsystem 200 comprises the device of regulating the operational condition in the conversion system, comprise the operational condition among the GQCS 20, therefore control the clean total output of conversion process, and be converted into during the gaseous product with particular chemical and physics component at coal, the setting point of reaction conditions is maintained in the variable specified range.This system can be automatization and be applicable to various gasification systems.

Control subsystem 200 can comprise following function.In one embodiment, reduction or the functional defect that replaces in GQCS 20 processes that control subsystem 200 can perception efficient, and with air flow divert alternate processes or standby regulation system.In another embodiment, control subsystem 200 can provide the device of finely tuning GQCS 20 steps and the optimum condition that smallest offset is provided.

Control subsystem 200 of the present invention can comprise the monitoring device 202 for the chemical composition of analyzing the air-flow that passes through GQCS 20, the gas flow of described process and thermal parameter; And setting device 206, for the component of the condition in the adjusting GQCS 20 with efficiency optimization and output gas.The adjusting of carrying out to reactant (for example, having the activated carbon injection of sufficient residence time, the pH control of sour gas washer) can be with making this process effectively carry out and carry out according to the optimised mode of design code.

The subsystem of adjustments of gas product

Coal gasification of the present invention system also is provided for the device of adjustments of gas product alternatively, for example, handle the chemical composition of gaseous product and regulate further feature by homogenizing, such as the flow of gaseous product, pressure and temperature to satisfy the requirement in downstream.This gaseous product regulon system 22 makes the continuous and stable air-flow that limits feature be passed to downstream application, such as gas turbine 24 or engine.

As understood by a person skilled in the art, gasification can produce the gas of component, temperature or flow velocity fluctuation.For the characteristic fluctuation that makes gaseous product minimizes, the gas regulating system 22 with the collection device form is set, it is used for the gaseous product that transmission has constant characteristic to upstream device.

In one embodiment, the invention provides gas regulating system 22, the gaseous product of this systematic collection gasification also weakens the chemistry fluctuation of the gaseous fraction in the chamber 25 that homogenizes etc.Other parts of system are the adjustments of gas feature alternatively, described feature such as flow, temperature and pressure so that its fall in the acceptable scope of downstream application.System's feature of adjustments of gas product by this has the continuous flow of constant characteristic with generation, is used for being passed to downstream application, such as gas blowing engine or gas turbine 24.

Especially, optional gaseous product regulon of the present invention system 22 provides gas (for example to homogenize chamber 25 (Fig. 1) or similar devices, the gas compressor 21 of Fig. 1 and 2, the gas storage 23 of Fig. 4 etc.), their size is designed to provide the residence time of the gas that homogenizes that is enough to obtain the constant output component.Other parts of this gas regulating system are designed to satisfy the gas performance requirement of downstream application.System comprises that also control subsystem 200 is with kinetics and the output of optimizing process.

The component of gaseous product that enters regulation system 22 of the present invention is determined in gasification.Make during the gasification and regulate to allow gaseous product to be optimized for specific end use (for example, gas turbine 24 or be used for the fuel cells applications 26 of generating).Therefore, the component of gaseous product can be formulated to (for example being used for specific energy generation technique, be used for specific gas engine or gas turbine 24), and dissimilar according to used coal and treatment additive, be used for best total transformation efficiency by the operating parameters of regulating gasification.

The gaseous product that leaves gasification system can be in the limited range of target components, and still, because the mutability of gasification such as coal component and filler speed, reaches airflow and temperature fluctuation, the characteristic of gaseous product can be along with time fluctuation.

Be similar to the control of gaseous product component, the flow velocity of gaseous product and temperature can be monitored, for example by monitoring device 202, and are controlled by in the gasification system, for example by setting device 206, in order to gas standard is maintained in the predetermined tolerance that is limited by terminal use.No matter these controls, the flow velocity of gaseous product and the fluctuation of temperature will take place along with the time.In flow rate conditions, these fluctuations can occur on the basis of second to second, and temperature is on the basis of per minute.

Gaseous product can be affected in regulation system of the present invention to the conversion of the gas of the specific components with requirement of satisfying application-specific equipment.Regulation system comprises the one or more gases chamber 25 that homogenizes, and this chamber 25 that homogenizes comprises gaseous product inlet device, adjustments of gas outlet unit and emergency exit alternatively.

The mixing that the chamber 25 of homogenizing of gaseous product receives the gaseous product that is produced by gasification system and promotes gaseous product is with any fluctuation of the chemical composition that weakens the gaseous product in the chamber 25 that homogenizes.Other gas characteristic also will be reduced in gaseous product mixing process such as the fluctuation of pressure, temperature and flow velocity.

So that described chamber or described size are minimised as purpose as far as possible, design the size of described chamber according to the requirement of the performance characteristic of upstream gasification system and downstream mechanism.The described gas chamber 25 that homogenizes is designed to receive gaseous product from gasification, and gas kept be enough to mixed gas a certain residence time to realize having the gas volume of constant chemical composition.

Residence time is the amount that gaseous product is directed to the time in the chamber 25 that homogenizes that is retained in before the upstream device.Residence time is proportional to proofread and correct the fluctuation of variable in the gasification reaction, in order to realize falling into the gaseous fraction that can accept in the tolerance value scope with the reaction times of relevant gasification system.For example, gaseous product is retained in whether the sufficiently long time falls within the tolerance of gaseous fraction with definite its in the chamber 25 that homogenizes, and described tolerance supplies specific downstream application, and gasification is made any adjusting depart from correction.

In addition, the residence time of gaseous product in the chamber 25 that homogenizes depends on the amount of the variable in the gaseous product feature.That is to say that the variation in the gaseous product feature is more little, it is more short to proofread and correct the required residence time of described variation in the chamber 25 that homogenizes.

Optional gas regulation subsystem 22 is designed to provide the residence time of abundance in the chamber 25 that homogenizes.In one embodiment, gas regulation subsystem 22 provides at least 1 second residence time.In another embodiment, gas regulation subsystem 22 provides no more than 2 seconds residence time.In another embodiment again, gas regulation subsystem 22 provides 2 to 10 seconds residence time.In another embodiment again, gas regulation subsystem 22 provides and reaches 30 seconds residence time.

The gas of discharging the adjusting of optional regulation system 22 of the present invention will have the stabilization feature, and these features satisfy the regulation of downstream application.Usually, the machinofacture merchant will provide that particular mechanical means allows and requirement well known by persons skilled in the art and tolerance.

The purposes of gasification system/described processing

Described system gasification of coal used according to the invention and make gasification, described method generally include coal are passed to step in the gasification reactor vessel 14, described coal in be heated herein, drying, and the volatile constituent in the dried feed is volatilized.In an embodiment of invention, the charcoal that the air of heating is used to further to drive gained is converted into its gaseous component fully, stays the cinder by product.The combination product of drying, evaporation and combustion step provides waste gas, and described waste gas also imposes heating described waste gas is converted into the hot gaseous product that comprises carbon monoxide, carbonic acid gas, hydrogen and steam by plasma heat source 15.Steam and/or air/oxidizer treatment additive 38 can optionally be added at gasifying stage and/or waste gas transformation stage.

In an embodiment of invention, described process also comprises by 44 pairs of by product cinders of second plasma heat source and imposes heating to form the slag product.

Process of the present invention also comprises the gaseous product of heat and by the step that heat exchange subsystem 18 transmits heat to be passed to refrigerant from hot gas.In one embodiment, refrigerant is air.In another embodiment, refrigerant is the oxygenant that is selected from oxygen or rich oxygen containing air.

Process of the present invention comprises alternatively the cooling gas product is delivered to step in second heat exchanger 18, and this step heat is passed to refrigerant from cooling gas, and described refrigerant is gaseous product and the steam of water to generate further cooling.

Process of the present invention makes clean transformation efficiency maximum by offsetting with the electric weight that is consumed, for example described electric weight heat, the driving rotating machinery device that forms the driving gasification, and article on plasma body heat source 15,44 energy supplies.For being that purpose is used to produce electricity, by the energy that will be consumed by total gasification with (for example use gaseous product, to gas turbine 24 or in 26 energy supplies of battery fuel technology) energy that generates determination efficiency recently mutually, and generate steam with to steam turbine 52 energy supplies by quick recovery of heat.

Gasification also can comprise correction (or feedback) control step, the variation that described control step is measured according to flow velocity, temperature and/or the component of gaseous product is regulated coal input speed, gaseous product flow velocity, air/oxidizer and/or steam treatment additive input speed, system pressure and is fed to one or more in the energy of plasma heat source.Therefore the feedback control step is held within the acceptable range flow velocity, temperature and/or the component of gaseous product.

In an embodiment of the invention, described process also is included in coal and adds before the gasification reactor vessel 14 step with its preheating to.

In one embodiment, gasification according to the present invention has adopted from add the purposes that warm air or other oxygenant gasification reactor vessel 14 be heated to be suitable for make the temperature of gasification of gas to air type heat exchanger 48.In this embodiment, with air be delivered in the system be usually system 10 the unloading phase use--add warm air so that the startup gas of heat to be provided by plasma heating, enter gas-air heat exchanger 48 after the described gas and add warm air with generation.The air of heating is passed to the heating atmospheric gas inlet unit so that gasification reactor vessel 14 is heated, and whole process like this can not used mineral fuel and moved.

Described invention is described referring now to specific embodiment.The following examples that are that to be understood mean description working of an invention mode and restriction invention never in any form.

Embodiment

Usually, use system of the present invention be by with coal with from such as plasma heat source 15, the heat that adds the source of any other thermal source that warm air maybe may be fit to etc. is delivered in the gasification reactor vessel 14, raw material is subjected to sufficient heating so that gasification reaction takes place in this container.

The heating of coal causes removing any residual moisture and evaporates any volatile constituent, and therefore the product char of partial oxidation is provided.Further hot spots oxidation product char makes charcoal be converted into its gaseous component fully, stays the cinder by product, can be further heated and change into slag after this by product.

Extra oxygen can be injected in the gasification reactor vessel so that produce the thermopositive reaction of carbon monoxide, carbonic acid gas and carbon granule and begin or accelerate.Thermopositive reaction increases processing treatment temperature in the gasification reactor vessel 14 with the heat that is provided by the heat treated air alternatively.

In one embodiment, the processing treatment temperature is between about 1000 ℃ to about 1300 ℃, even lower or higher temperature also can be considered.In an embodiment of the invention, the average gasification temperature in the gasification reactor vessel of described process use is about 1100 ℃+/-100 ℃.

Reform

The waste gas that forms in gasification reactor vessel 14 can further heat also alternatively with steam treatment with plasma heat source 15.These reactions mainly are thermo-negative reaction.In an embodiment of the invention, to be maintained at for reaction being remained on the minimized proper level of generation that makes pollution when guaranteeing to be converted into the specific gas product fully be sufficiently high scope to temperature.In one embodiment, temperature range is from about 900 ℃ to about 1300 ℃.The proper temperature scope can easily be determined by the technician.

The vapor action that is added in the reforming step is to guarantee to form the gaseous product with specific components, also reduces the outflow temperature of gas simultaneously.In one embodiment, the relief outlet temperature of gaseous product is reduced between about 900 ℃ to about 1200 ℃.In another embodiment, the relief outlet temperature of gaseous product is reduced to 1000 ℃+/-100 ℃ medial temperature.

In an exemplary embodiment, on the basis of the component of the relief outlet temperature of monitoring relief outlet synthesis gas flow velocity, relief outlet synthesis gas and relief outlet gas, determine coal, oxygen, steam and be fed to the amount of the energy of plasma heat source 15.

Specifically with reference to Figure 15 and 16, together be transfused in the first processor (by box 30 explanations) by the flow velocity numerical value of the carbon monoxide in the exit gas of circuit 100 and 102 and carbonic acid gas and the filler speed numerical value of the coal in the circuit 104 (for example, obtaining by setting device 206-1).First processor 30 is estimated the carbon amount in the gasification reactor vessel 14 and the filler speed of regulating coal accordingly.

The output valve of pass through circuit 106 of the first processor of measuring from the percentages that carbon monoxide and carbonic acid gas are provided 30 and the percentages of the hydrogen that passes through circuit 108, with steam by circuit 110 (for example, by setting device 206-2) and oxygen (for example, by setting device 206-3) numerical value be transfused to second treater (by box 32 explanation) together.Second treater 32 estimates that the input of new oxygen and steam is to realize specific gas component.

, represent numerical value with the input of Outlet Gas Temperature by circuit 114 and together be transfused in the 3rd treater 34 by circuit 112 from the output valve of second treater 32.The 3rd treater 34 calculates new plasma heat source (for example, plasmatorch), and described work output is as the output rating (for example, being sent to setting device 206-4) of passing through 116.

The fusing of by product cinder

In an embodiment of invention, the solid cinder by product of charcoal combustion step is also alternatively by handling with the fusing of second plasma heat source 44.When being entrained in the molten slag bath, particle allow grace time to guarantee that all volatile matters and carbon are removed fully.As persons skilled in the art will recognize, residence time is the function of particle size.The heat that is produced by second plasma heat source 44 homogenizes slag and allows it to be sucked out in heat.Plasma heat source 44 is heated to temperature between about 1100 ℃ to about 1600 ℃ with slag.In one embodiment, temperature is between about 1400 ℃ to about 1650 ℃.The operation of this temperature distribution can help avoid wasted heat and after the water of slag in the bottom of cool gasification reaction vessel 14.

Even invention is described with reference to some embodiment, its different modification is to show and the purport and the scope that do not depart from the invention that goes out as claims institute summary of suggestion for those skilled in the art.

Following examples have been set to two kinds of grizzles of comparison--and the synthesis gas that brown coal and sub-bituminous coal (seeing Table 1) produce, described gas have the calorific value that is suitable for integrated gasification combined cycle (IGCC) generating.

Below two embodiment be set to prove and provide the synthesis gas that is suitable in IGCC, using required operating parameters that wherein said Combined Cycle comprises a gas turbine (42MW) and a steam turbine.In the present embodiment, select the conduct of GE MS6001B Combined Cycle to be used for the object module of both of these case: clean plant capacity output is about 64MW.According to present embodiment, the total efficiency of Combined Cycle can arrive more than 45%, far above traditional coal powerplant (30-33%).

Gasification reactor vessel can based on or take stream (entrained flow) or the reactor of thermopnore type, air separation equipment (ASU) will provide 95% oxygen as main oxygenant.Solid residue will at high temperature be converted into slag by plasmatorch.The unstripped gas of coming out from transmodulator is cooled before further such as gas cleanup step such as fine particle and removal of sulphurs and washs.Cleaning and the synthesis gas that is conditioned will be transported in the gas turbine and burning produces.The flue gas of high-temp combustion is introduced into heat recovery steam producer (HRSG), and it provides steam for steam turbine, improves the ability that produces electricity.

The component of table 1 brown coal and sub-bituminous coal

The type of coal

C

H

O

N

S

Humidity

HHV Btu/lb

Brown coal

40.6％

6.9％

45.1％

0.6％

0.9％

36％

7000

Sub-bituminous coal

50.5％

6.2％

35.5％

0.7％

0.3％

25％

8560

Press: C, H, O...... partly are according to weight

Brown coal are as raw material

Gasification reactor vessel is operated under the pressure in the scope from 2atm to 10atm under the temperature in 1000 ℃ to 1100 ℃ scope.The input speed of coal was controlled in 1309T/ days and was dried to humidity in advance and is lower than 10%.The oxygenant that adopts is the oxygen of 95% purity, and the oxygenant input speed of about 205SCFM (463T/ days) is set.Purify and cooled synthesis gas by 35.6% H ₂Form with 31.4% CO, have 9.1MJ/m ³Calorific value.The volumetric flow rate of the synthesis gas of dried and clean is about 47,323m ³/ hr.Count there being how many energy to be transferred to synthesis gas from solid fuel, the efficient of cooling gas is about 85%.

Sub-bituminous coal is as raw material

Gasification reactor vessel is operated under the pressure of 2atm in the scope of 10atm under 1100 ℃ medial temperature.The input speed of coal was controlled in 617T/ days and was dried in advance and is lower than 10% humidity.The oxygenant that adopts is the oxygen of 95% purity, and the input speed of about 85SCFM (127T/ days) is set.Purify and cooled synthesis gas by 45.0% H ₂Form with 30.5% CO, have 10.2MJ/m ³Calorific value.The volumetric flow rate of dry synthesis gas is about 51,400m ³/ hr.The efficient of the cooling gas of gasification system is about 86%.

As by being pointed out, make sub-bituminous coal and brown coal hydrogasification will consume more as the oxygen of oxygenant with the gasification that has relatively proved brown coal of the gas that produces similar calorific value and produce still less synthesis gas for gas turbine; This means and sub-bituminous coal relatively, more brown coal will be required to produce same amount.Brown coal also are lower than the desired efficient of sub-bituminous coal as the cooling gas efficient of raw material.But present embodiment points out that this gasification system can be used to grizzle is converted into the synthesis gas with the calorific value that is applicable to that the IGCC energy produces.

Integral body is incorporated in all patents in this specification sheets, comprises that the open of public publication of disclosed patent application and master data is incorporated herein in full as a reference with it especially, and it is special and point out individually by with reference to being incorporated herein that its degree is similar to each above-mentioned independent patent, public publication and master data.

Claims (12)

1. system that is used for coal is converted into the gas of specific components, it comprises:

Gasification reactor vessel, it comprises one or more treatment zones, one or more plasma heat source, is used for adding coal the one or more coal input units of described gasification reactor vessel to adjustable coal filler speed, and one or more outlet for output gas;

The solid residue processing subsystem, described solid residue processing subsystem comprises solid residue surge chamber, plasma heating device and slag take-off equipment;

Gaseous mass regulon system;

Integrated control system, it comprises:

The system monitoring device produces data for measuring one or more system parameters,

Calculating device is used for collecting and analyzing the described data that produced by described system monitoring device, and

Take-off equipment, it sends proper signal and is positioned in the described system variation in everywhere the one or more systematic regulators with influence,

Wherein, described Controlling System is monitored described one or more system parameter and is sent a signal to described suitable systematic regulator influencing the variation in the described one or more systematic regulator, and therefore produces the gaseous product of specific components.

2. system according to claim 1, further comprise the heat recuperation subsystem, wherein said heat recuperation subsystem comprises that one or more gases are to the air type heat exchanger, with described gaseous product is passed to described one or more gas to the device of air type heat exchanger, wherein said transfer device is communicated with described one or more output pneumatic outlet fluids.

3. system according to claim 2, wherein said heat recuperation subsystem further comprises one or more heat recovery steam producers and described gaseous product is passed to the device of described one or more heat recovery steam producers.

4. according to the described system of claim 1 or 2, wherein said gaseous mass regulon system comprises one or more particulate matter removal devices, sour gas removal device, heavy metal removal device and be used for regulating the device of humidity and the temperature of described gas when described gas passes described gaseous mass regulon system.

5. system according to claim 1 further comprises gaseous product regulon system.

6. system according to claim 5, wherein said gaseous product regulon system is the homogenization jar.

7. system according to claim 1, wherein said system also comprises the treatment additive input unit, described treatment additive input unit be one or more steam-ins, one or more oxidant inlet or comprise aforementioned both.

8. system according to claim 7, wherein said oxygenant is air, oxygen or rich oxygen containing air.

9. method that is used for coal is converted into the gaseous product with specific components said method comprising the steps of:

With the coal input speed coal is delivered in the gasification zone;

With the treatment additive input speed treatment additive is delivered in the described gasification zone;

Make described coal stand heating so that waste gas and by product cinder to be provided;

Described waste gas is passed to the zone of reforming;

Heat described waste gas with plasma heat source;

Add steam to described waste gas so that described waste gas is converted into synthesis gas with the steam input speed;

Described by product cinder is passed to the melting range;

The plasma heat source of regulating by slag makes described by product cinder accept heating so that described by product cinder is converted into slag and described slag is maintained melting condition;

Described fusing slag is discharged from described melting range, and

Allow described fusing slag to cool off to provide glassiness slag.

10. method according to claim 9, further comprise the correction feedback step, one or more during described correction feedback step comprises the following steps: monitor the component of described gaseous product step, the described gaseous product of monitoring the step that flows and monitor the step of the temperature of described gaseous product.

11. method according to claim 10, wherein said correction feedback step further comprise the steps: to regulate one or more so that specific gas product component to be provided in described coal input speed, oxygen input speed and the described steam input speed.

12. method according to claim 10, wherein said correction feedback step further comprise the steps: to regulate one or more to solve the variation that records in the described synthesis gas component in described coal input speed, oxygen input speed and the described steam input speed.

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