CN103965965A

CN103965965A - System and method for gasification

Info

Publication number: CN103965965A
Application number: CN201410033764.0A
Authority: CN
Inventors: R.A.德皮伊
Original assignee: General Electric Co
Current assignee: Air Products and Chemicals Inc
Priority date: 2013-01-24
Filing date: 2014-01-24
Publication date: 2014-08-06

Abstract

A system includes a gasifier having a first enclosure having a first inlet, a first outlet, and a first interior volume. The first inlet is configured to receive a first fuel feedstock into the first interior volume, and the first outlet is configured to output a first syngas away from the first interior volume. The system also includes a plasma gasifier disposed downstream from the first outlet and coupled to a waste stream produced by the gasifier from the first fuel feedstock.

Description

For the system and method gasifying

The cross reference of related application

The application is the U.S. Patent application No.12/683 that is entitled as " System for RemovingFine Particulates From Syngas Produced by Gasifier(for remove fine grain system from the synthetic gas being produced by gasifier) " submitting on January 6th, 2010,413 partial continuous application, the mode that described application is quoted is in full incorporated to herein.

Technical field

Theme disclosed herein relates to gasification system, relates more particularly to improved particle removal system and method.

Background technology

Integrated gasification combined cycle plants (IGCC) power station can be from various carbon raw materials (as coal or Sweet natural gas) relatively clean and generate energy effectively.IGCC technology can by gasifier with oxygen and steam reaction and carbon raw material is converted into carbon monoxide (CO) and hydrogen (H ₂) mixture, i.e. synthetic gas.This power station is clean and processing gas conventionally, with the fuel as in downstream application.But the gaseous mixture being produced by gasifier contains the particle of significant quantity conventionally, described particle can comprise the organic materials of inorganic pollutant and unconverted.Unfortunately, before can utilizing synthetic gas, these particles must make to wash with water out conventionally, use ceramic filter to go out, and use cyclonic separator to eliminate, or remove via other method.The carbonaceous particle of the unreacted being dropped in addition, can reduce the carbon conversion efficiency of this gasification system.

Summary of the invention

Some embodiment that scope is identical with the present invention of primitive request protection is summarized as follows.These embodiment are not intended to limit the scope of the present invention for required protection, and on the contrary, these embodiment only aim to provide the short summary of possibility form of the present invention.In fact, the present invention can be contained various ways that can be similar or different from embodiment as described below.

In the first embodiment, a kind of system comprises the gasifier with the first shell, and described the first shell has the first entrance, the first outlet and the first internal volume.Described the first entrance can receive the first fuel feedstocks and enter described the first internal volume, and described the first outlet can be exported the first synthetic gas from described the first internal volume.Described system also comprises plasma gasification device, and described plasma gasification device is arranged at the downstream of described the first outlet, and is attached to the waste streams being produced by described the first fuel feedstocks by gasifier.

In a second embodiment, one method is included in gasifier and gasifies the first fuel feedstocks to produce the first synthetic gas and waste streams, the described waste streams of filtration to produce the second fuel feedstocks, and in plasma gasification device, processes described the second fuel feedstocks to produce the second synthetic gas.

In the 3rd embodiment, a kind of system comprises the instruction being arranged on nonvolatile machine readable media.Described instruction is configured to gasify the first fuel feedstocks in gasifier to produce the first synthetic gas and waste streams, the described waste streams of filtration to produce the second fuel feedstocks, and in plasma gasification device, processes described the second fuel feedstocks to produce the second synthetic gas.

Brief description of the drawings

In the time reading following detailed description in detail with reference to accompanying drawing, these and other features of the present invention, aspect and advantage will become better understood, and in whole accompanying drawing, same Reference numeral represents same parts, wherein:

Fig. 1 is the block diagram of an embodiment in integrated gasification combined cycle plants (IGCC) power station with particle removal system;

Fig. 2 is the block diagram that comprises an embodiment of the gasification system as shown in Figure 1 of particle removal system (it comprises plasma torch system);

Fig. 3 is the block diagram that is included in an embodiment of the gasification system as shown in Figure 1 of the plasma gasification device in the downstream of non-plasma base gasifier;

Fig. 4 is the block diagram that is included in an embodiment of the gasification system as shown in Figure 1 of the plasma gasification device in the downstream of syngas cooler;

Fig. 5 is the block diagram that is included in an embodiment of the gasification system as shown in Figure 1 of the plasma gasification device in the downstream of gas cleaning unit;

Fig. 6 is the block diagram that comprises an embodiment of the gasification system as shown in Figure 1 of plasma system, and described plasma system is along the install pipeline that gasifier is attached to syngas cooler;

Fig. 7 is the cross-sectional side view that comprises an embodiment of the plasma gasification device of the plasma flow of multiple convergences;

Fig. 8 is the cross-sectional view of an embodiment of the plasma gasification device that obtains along the line 8-8 of Fig. 7, and it shows the plasma torch system of the plasma flow with convergence;

Fig. 9 is the cross-sectional view of an embodiment of the plasma gasification device that obtains along the line 8-8 of Fig. 7, and it shows the plasma torch system of the plasma sheet with convergence;

Figure 10 is the block diagram of an embodiment in integrated gasification combined cycle plants (IGCC) power station with powder treatment system; And

Figure 11 is the block diagram that comprises an embodiment of the gasification system as shown in figure 10 of powder treatment system (it comprises plasma torch system).

Embodiment

One or more specific embodiment of the present invention will be described as follows.For the simple and clear description of these embodiment is provided, actual all features of implementing may not described in specification sheets.Should be appreciated that in any this actual exploitation of implementing, as in any engineering or design item, must carry out decision that much enforcement is relevant to realize developer's specific objective, as meeting the relevant restriction relevant with business of system, an enforcement may be different from the specific objective of another enforcement.In addition, should be appreciated that this development ability may be complicated and consuming time, but the normal work to do that remains design, assembling and manufacture for thering are those skilled in the art of benefit of the present disclosure.

In the time introducing the member of each embodiment of the present invention, article " ", " described " are intended to mean to exist one or more members.Term " comprises ", " comprising " and " having ", to be intended to be comprising property, and means to exist the other key element except listed key element.

As discussed below, the embodiment of particle removal system uses focus energy (for example plasma physical efficiency) to process the gained fluid stream from gasifier.As used herein, focus energy is at least greater than about 5MJ/m ³.For example, focus energy can be about 10MJ/m ³to 70MJ/m ³between.For other example, in one embodiment, plasma body can have about 50MJ/m ³energy density.Focus energy system as herein described can comprise one or more focus energy equipment that can produce and guide one or more focus energy bundles or sheet.For example, particle removal system can comprise plasma torch system, and described plasma torch System Construction is that the one or more plasma flows that are derived from one or more plasma torchs are guided to fluid stream.In this way, focus energy system (for example plasma torch) can be for example by making inorganic particle fusing and making organic granular reaction cause the change of fluid composition.Therefore,, in the time of rare gas element process torch, plasma torch can be retained to the internal temperature of much approximately 5000 DEG C.For example, the internal temperature in plasma torch can at least be greater than about 2000 DEG C, 3000 DEG C, 4000 DEG C or 5000 DEG C.As used herein, plasma body may be defined as and can reach any part ionized gas that is enough to melt inorganic particle and/or makes the temperature of organic granular reaction.In addition, as used herein, plasma torch may be defined as any equipment that can produce by its nozzle the oriented flow of plasma body.The aforementioned feature of particle removal system can be conducive to increase carbon conversion efficiency in relevant gasification system, because keep unreacted organic granular still can react in particle removal system after the gasification of the non-plasma base in gasifier.Therefore, the particle removal system of uniqueness as herein described can allow gasification system to produce the available synthetic gas of maximum from raw material supply.In addition,, due to the high-density of inorganic byproduct, particle removal system can be conducive to more easily to separate the pollutent of available synthetic gas and available synthetic gas.

In certain embodiments, particle removal system can comprise plasma gasification device, and described plasma gasification utensil has and is arranged at the indoor one or more focusing energy (for example plasma torch) of plasma gasification.Plasma torch can be guided through plasma flow plasma gasification chamber to fluid and flow.For example, plasma gasification device can comprise shell, and described shell has the one or more plasma torchs that are attached to shell.In such an embodiment, plasma torch can be directed toward each other, roughly to assemble plasma flow.In addition, one or more plasma torchs can be set, to guide one or more plasma flows in the updrift side relative with the downstream direction of fluid stream.In other embodiments, plasma torch system for example can be arranged at, in the lower region (downstream area) of non-plasma base gasifier.For example, plasma torch can be arranged in the first adjacent region of outlet with gasifier, described region be at least less than gasifier internal volume about 30%.For other example, particle removal system can be attached to the downstream of downstream, water treatment system of outlet, the gas cleaning unit of syngas cooler or associated with water treatment system, or any other suitable position in gasification system.

In certain embodiments, as below discussed about Figure 10 and 11, powder treatment system can be processed the gained waste streams being produced from the first fuel feedstocks by non-plasma gasifier with plasma gasification device as discussed above, to produce the second synthetic gas.Therefore, can increase the carbon conversion efficiency of gasification system, thereby and owing to no longer needing waste streams to be transmitted back to non-plasma gasifier and can to eliminate or reduce processing and the recovery of waste streams.In addition, powder treatment system can allow the operator of factory with following mode operation factory: efficiency of carbon conversion is for example, lower in non-plasma gasifier (pressing down in oxygen environment), because any unreacted carbon that powder treatment system can be converted from non-plasma gasifier is to produce synthetic gas.Therefore, the overall efficiency of carbon conversion of factory can remain under required level.

Fig. 1 is the diagram of an embodiment of integrated gasification combined cycle plants (IGCC) system 100 of the synthesis gas (being synthetic gas) that can produce and burn.The element of IGCC system 100 can comprise the fuel source 101 can be used as for the energy of IGCC, as feeding-in solid body.Fuel source 101 can comprise coal, refinery coke, biomass, wood based material, agricultural waste, tar, coke-oven gas and pitch, or other carbonaceous materials.Although the embodiment of particle removal system has been shown in the whole context of IGCC system 100, particle removal system disclosed herein can be used in any person of polytype factory of use or generation synthetic gas.For example, particle removal system can be used for producing in any factory of CO, hydrogen, methyl alcohol, ammonia or any other chemistry or fuel product., particle removal system as herein described can with together with the factory IGCC factory, use.In addition, in certain embodiments, can use the particle removal system of unpowered generation (for example generator).

The solid fuel of fuel source 101 can be passed to feed preparation unit 102.Feed preparation unit 102 is can be for example broken by fuel source 101 is cut, grind, shred, grind, briquetting or granulation and fuel source 101 is adjusted to size or reshaped, to produce raw material.In addition, water or other suitable liquid can be added into the fuel source 101 in feed preparation unit 102, to produce slurry feedstock.In other embodiments, liquid is not added into fuel source, therefore generates dried feed.

Raw material can be passed to gasifier 104 from feed preparation unit 102.Gasifier 104 can be synthetic gas by feedstock conversion, the combination of for example carbon monoxide and hydrogen.This conversion can realize in the following way: depend on the type of gasifier used 104, make raw material stand steam and the oxygen of for example, controlled quatity under high pressure (about 20 bar to 85 bar) and high temperature (about 700 DEG C to 1600 DEG C).Gasification can comprise the raw material that experiences pyrolytic process, the heating raw by described pyrolytic process.Depend on the fuel source 101 for generation of raw material, the temperature in pyrolytic process in gasifier 104 can be about 150 DEG C to 700 DEG C.Can produce solid (for example charcoal) and residual gas (for example carbon monoxide, hydrogen and nitrogen) in the heating of pyrolytic process Raw.Can be only about 30% of initial feed weight from the weight from the remaining charcoal of raw material of pyrolytic process.

Then can in gasifier 104, carry out combustion processes.Burning can comprise oxygen is introduced into charcoal and residual gas.Charcoal and residual gas can be with oxygen reaction to form carbonic acid gas and carbon monoxide, and this provides the heat for gasification reaction subsequently.Temperature in combustion processes can be about 700 DEG C to 1600 DEG C.Then, can in gasification step process, steam be introduced in gasifier 104.Charcoal can with carbonic acid gas and steam reaction, to be created in carbon monoxide and the hydrogen at the temperature of about 800 DEG C to 1100 DEG C.In fact, gasifier utilizes steam and oxygen so that some in raw material are produced carbon monoxide and release energy by " burning ", and this has driven the second reaction, and described the second reaction is further hydrogen and other carbonic acid gas by feedstock conversion.

In this way, gained gas makes by gasifier 104.This gained gas can comprise carbon monoxide and the hydrogen of about 85% equal proportion, and CH ₄, HCl, HF, COS, NH ₃, HCN and H ₂s(is in the sulphur content of raw material).This gained gas can be described as dirty synthetic gas or untreated synthetic gas, because it contains for example H ₂s.Gasifier 104 also can produce the refuse that can be moistening inorganic materials, as slag 109.This slag 109 can shift out from gasifier 104, and for example processes as roadbase or as another material of construction.

Particle removal system 106 can be attached to one or more parts of IGCC system 100, as having in the region 107 of gasifier 104 and gas cleaning unit 110.For example, particle removal system 106 can be attached to the downstream part of gasifier 104, or in the downstream of the outlet of gasifier 104.Further for example, particle removal system 106 can be attached to any other parts in syngas cooler, gas cleaning unit 110, unit for treating water or IGCC system 100.In other words, particle removal system 106 is arranged at the downstream of the main gasification zone (for example non-plasma gasification) of gasifier 104.Particle removal system 106 comprises focus energy system, as plasma torch system 108.Focus energy system (for example plasma torch system 108) can provide high-energy focusing bundle, if energy density is about 50MJ/m ³bundle.Plasma torch system 108 can comprise one or more plasma torchs, and described one or more plasma torchs are configured to for example, remove particle from the fluid in the downstream of the main gasification zone of gasifier 104 (unreacted synthetic gas).That is, plasma torch system 108 is configured to melt inorganic particle, and organic granular in the gained gas that makes to be made by gasifier 104 reacts.In certain embodiments, inorganic particle and organic granular can have the median size that is less than about 80mm.For example, particle can have about 500 microns to the median size between 100mm.One or more plasma torchs can be any torch that can produce the plasma body that is applicable to gasification.For example, can comprise can received current and produce two electrodes of electric arc for plasma torch.In the time of rare gas element process electric arc, plasma torch can be retained to the internal temperature of much approximately 5000 DEG C.For example, the internal temperature in plasma torch can at least be greater than about 2000 DEG C, 3000 DEG C, 4000 DEG C or 5000 DEG C.Above-mentioned parts can be conducive to increase the carbon conversion efficiency in IGCC system 100, because keep unreacted organic granular still can react in particle removal system 106 after the gasification in gasifier 104.This can make IGCC system 100 can make the amount of the available synthetic gas producing from raw material reach maximum.In addition,, than conventional system, this system 106 and 108 can produce finer and close inorganic byproduct, is conducive to thus the synthetic gas that more easily separated from contaminants from available synthetic gas can be used.

Gas cleaning unit 110 is configured to the clean unreacted synthetic gas from gasifier 104.Gas cleaning unit 110 can wash unreacted synthetic gas, to remove HCl, HF, COS, HCN and H from unreacted synthetic gas ₂s, its can comprise by the sour gas in sulphuring treatment device 112 for example remove process and in sulphuring treatment device 112 separate sulfur 111.In addition, gas cleaning unit 110 can be via unit for treating water 114 from unreacted synthetic gas separated salt 113, described unit for treating water 114 can utilize desalt technology to produce available salt 113 from unreacted synthetic gas.In certain embodiments, unit for treating water 114 comprises particle removal system 106 and/or plasma torch system 108.Subsequently, can comprise clean synthetic gas or treated synthetic gas from the gas of gas cleaning unit 110, (for example, sulphur 111 has been removed from synthetic gas), and there are other chemical of trace, for example NH ₃(ammonia) and CH ₄(methane).

Gas processer 116 can be used for from treated synthetic gas, removing residual gas component 117, as ammonia and methane, and methyl alcohol or other residue chemistry product.But, from treated synthetic gas, remove residual gas component 117 for optional, even for example, because in the time containing residual gas component 117 (tail gas), treated synthetic gas also can be used as fuel.At this moment, treated synthetic gas can comprise about 40% CO, about 55% H ₂with about 3% CO ₂, and substantially removed H ₂s.Can transfer to using this treated synthetic gas as ignitable fuel the burner 120 of gas turbine engine 118, for example combustion chamber.In addition, can before transferring to gas turbine engine, from treated synthetic gas, remove CO ₂.

IGCC system 100 also can comprise air gas separation unit (ASU) 122.ASU122 can operate taking by for example distillation technique by air separation as component gas.ASU122 can be from being supplied to oxygen separation its air by supplementing air compressor 123, and ASU122 can be passed to gasifier 104 by separated oxygen.In addition, ASU122 can transfer to separated nitrogen thinner nitrogen (DGAN) compressor 124.

DGAN compressor 124 can at least be compressed to the stress level that equals burner 120 by the nitrogen receiving from ASU122, not hinder the suitable burning of synthetic gas.Therefore,, once nitrogen is fully compressed to proper level by DGAN compressor 124, DGAN compressor 124 can transfer to compressed nitrogen the burner 120 of gas turbine engine 118.For example, nitrogen can be used as thinner to be conducive to control discharge.

As previously mentioned, compressed nitrogen can transfer to from DGAN compressor 124 burner 120 of gas turbine engine 118.Gas turbine engine 118 can comprise turbine 130, drive shaft 131 and compressor 132 and burner 120.Compressor 120 can receive fuel, and as synthetic gas, described fuel can spray from fuel oil atomizer under pressure.This fuel can mix with compressed air and from the compressed nitrogen of DGAN compressor 124, and in the interior burning of burner 120.Described burning can produce hot pressurised exhaust gas.

Burner 120 can guide to waste gas the exhaust outlet of turbine 130.When waste gas from burner 120 is during through turbine 130, waste gas forces turbine blade in the turbine 130 axis rotating driveshaft 131 along gas turbine engine 118.As shown, drive shaft 131 is connected to the various parts of gas turbine engine 118, comprises compressor 132.

Drive shaft 131 can be connected to turbine 130 compressor 132 to form rotor.Compressor 132 can comprise the blade that is attached to drive shaft 131.Therefore, in turbine 130, the rotation of turbine blade can make turbine 130 be connected to the blade in drive shaft 131 rotary compressors 132 of compressor 132.Described blade rotary in compressor 132 makes compressor 132 compress the air receiving via the air inlet in compressor 132.Then, compressed air can be fed to burner 120, and mixes to allow more high efficiency burning with fuel and compressed nitrogen.Drive shaft 131 also can be connected to load 134, and it can be permanent load, as the generator for for example produce electric power in power station.In fact, load 134 can provide for the rotation output by gas turbine engine 118 any suitable equipment of power.

IGCC system 100 also can comprise steam turbine engines 136 and recovery of heat steam generation (HRSG) system 138.Steam turbine engines 136 can drive the second load 140.The second load 140 also can be the generator for generation of electric power.But the first and second loads 134,140 can be the load of the other types that can drive by gas turbine engine 118 and steam turbine engines 136.In addition, although as shown shown in embodiment, gas turbine engine 118 and steam turbine engines 136 can drive point other load 134 and 140, but gas turbine engine 118 and steam turbine engines 136 also can be connected, utilization is to drive single load via single axle.The concrete structure of steam turbine engines 136 and gas turbine engine 118 can be concrete enforcement, and can comprise the arbitrary combination of part.

System 100 also can comprise HRSG138.The waste gas through heating from gas turbine engine 118 can be delivered to HRSG138 and for heating water, and produce and be used to steam turbine engines 136 that the steam of power is provided.Can will guide to condenser 142 from for example waste gas of the low-pressure section of steam turbine engines 136.Condenser 142 can utilize cooling tower 128 to be exchanged into refrigerated water through the water of heating.Cooling tower 128 is for water coolant being provided to condenser 142, to assist condensation to transfer to the steam of condenser 142 from steam turbine engines 136.Can transfer the condensation product of self cooling condenser 142 in the future and guide to HRSG138.Again, also can will guide to HRSG138 from the waste gas of gas turbine engine 118, to heat from the water of condenser 142 and to produce steam.

In the combined cycle system such as IGCC system 100, hot waste gas can flow and be passed to HRSG138 from gas turbine engine 118, and at HRSG138 place, hot waste gas can be used for producing high-pressure and high-temperature steam.The steam being produced by HRSG138 can produce for power through steam turbine engines 136 subsequently.In addition, also the steam supply of generation extremely can be able to be used to any other process of steam, as be supplied to gasifier 104.Gas turbine engine 118 power generation cycle are often called " to top circulation (topping cycle) ", and steam turbine engines 136 power generation cycle are often called " end circulation (bottoming cycle) ".By combining these two circulations (as shown in Figure 1), IGCC system 100 can produce larger efficiency in two circulations.Especially, can trap from the used heat to top circulation, and use it for and be created in the end steam used that circulates.

Fig. 2 is the block diagram of an embodiment of gasification system or process 150, and it comprises have focus energy system unique particle removal system 106 of (for example plasma torch system 108).Gasification system 150 can use partial oxidation gasification (for example texaco gasification process (TGP)) with from liquid hydrocarbon, petroleum residue, coke or their combination results synthesis gas.But particle removal system 106 can be used together with the gasification of multiple other types.For example, particle removal system 106 especially can be suitable for using together with the E-gas vaporization process of shell coal gasification course (SCGP), Concophillips Company and Mitsubishi Heavy Industries Ltd (MHI) dry feed gasifications etc.

Shown gasification system 150 comprises raw material preparation system or process 152, gasifier 104, syngas cooler 154, powder or slag removal system or process 156, particle removal system 106 and gas cleaning unit 110.Shown raw material preparation system 152 comprises the coal grinding machine 158, slurry tank 164 and the mashing pump 166 that are configured to receive water 160 and coal 162.Powder or slag remove system 156 comprise valve 168 and 170 and one or more lock hopper 172 to collect and/or to carry slag 109.Gas cleaning unit 110 comprises the water scrubber 174, valve 178, Heisui River 180 and the recirculation loop 182 that produce through the synthetic gas 176 of washing.

Gasifier 104 comprises the first entrance 186, the first outlet 188 and shell 190.Shell 190 limits such as upstream portion of the first internal volume 192(), described the first internal volume 192 can serve as main vaporizer in operating process.Distance 194 limits the height of the first internal volume 192.The such as downstream part of lower region 196(of gasifier 104) adjacent with the first outlet 188, and limited by height 198.The lower region 196 of gasifier 104 can at least be less than the first internal volume 192 or gasifier 104 whole volume about 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40% or 45%.The first pipeline 200 is attached to the first outlet 188 of gasifier 104 the second entrance 202 of syngas cooler 154.Shell 204 limits the second internal volume 206 of syngas cooler 154.Syngas cooler 154 is attached to second pipe 210 by the second outlet 208.Syngas cooler 154 is attached to powder in the 3rd outlet 212 or slag is removed system 156.

In the embodiment shown, gasifier 104 is for being applicable to the airflow bed gasification furnace in TGP., in gasification, the service temperature of gasifier 104 can be about 1200 DEG C to 1500 DEG C, and working pressure can be less than about 27 to 80 bar.Therefore, gasifier 104 can comprise refractory lining, and described refractory lining serves as inertia thermoshield in operating process.This refractory lining can by can bear at the most or be greater than about 500 DEG C, 1000 DEG C, 1500 DEG C or even the multiple refractory materials of temperature of 2000 DEG C make., refractory lining can be by keeping any material of its predetermined physical and chemical property to make when being exposed to this high temperature lower time.Can comprise pottery (for example clay or mineral substance), metal (for example titanium, tungsten), ceramic metal (i.e. the matrix material of pottery and metal) for the suitable refractory materials of gasifier 104, or other refractory materialss (for example silicon-dioxide, aluminum oxide).

In the embodiment of the gasification system 150 illustrating herein and describe, gasifier 104 is airflow bed gasification furnace, and wherein gained synthetic gas leaves gasifier 104 via the first outlet 188 that is positioned at gasifier 104 bottoms.But, it should be noted that uniqueness disclosed herein particle removal system 106 can with comprise that its middle outlet is not arranged at together with multiple other gasifications of gasifier of the base section of gasifier and use.For example, the disclosed embodiments can be combined with fixed bed gasifiers or fluidized-bed gasifier.In such an embodiment, the direction that flows through gasifier can be upwards, and gained synthetic gas can be left via the outlet that is positioned at the top section of gasifier or approaches the top section of gasifier.Further for example, particle removal system 106 can be used together with other airflow bed gasification furnaces, is wherein being set up and is flowing in direction upwards roughly by gasifier.

Particle removal system 106 comprises plasma torch system 108.The particle removal system 106 of Fig. 2 can be positioned at multiple positions of gasification system 150.For example, particle removal system 106 can be positioned at the such as downstream part of lower region 196(of the gasifier 104 adjacent with the first outlet 188), as shown in arrow 214.In such an embodiment, plasma torch system 108 can comprise the multiple plasma torchs that arrange around the circumference of lower region 196, or is arranged at the individual plasma torch in lower region 196.In other words, particle removal system 106 can be positioned at the non-plasma base gasifier 104 in downstream, main gasification zone (for example non-plasma base gasification).Further for example, particle removal system 106 can be attached to the first pipeline 200 between the first outlet 188 and second entrance 202 of syngas cooler 154 of gasifier 104, as shown in arrow 216.In such an embodiment, the one or more plasma torchs that are included in plasma torch system 108 can be arranged in the first pipeline 200 or be positioned on the first pipeline 200.For example, multiple plasma torchs can be along the wall setting of the first pipeline 200.Plasma torch can be to be applicable to melting inorganic particle and any mode of the organic granular reaction in synthetic gas arranged.For example, plasma torch can be directed toward each other, makes to assemble at predetermined point place from multiple plasma flows of plasma torch.In a further embodiment, particle removal system 106 can be positioned at any suitable position in the downstream of syngas cooler 154, as shown in arrow 218.For example, plasma torch system 108 can be connected to second pipe 210, and described second pipe 210 is attached to the second outlet 208 of syngas cooler 154.Further for example, plasma torch system 108 can be attached directly to syngas cooler 154.

In operating process, raw material preparation system 152 is prepared the slurry feed of the coal of about 50% to 70% weight in water.Particularly, water 160 and coal 162 are inputed in coal grinding machine 158.Coal 162 is crushed to more small-particle by coal grinding machine 158, and described particle is mixed to form the slurry feed of coal in water with water 160.Then described slurry feed is passed to slurry tank 164 to store before using.Mashing pump 166 enters the slurry feed in slurry tank 164, and the amount that is applicable to gasification 150 is passed to gasifier 104 via pipeline 220.Therefore, mashing pump 166 can be with continuous mode (being the slurry feed of mashing pump 166 per minute supply set amounts), progressively pattern (being the amount of slurry 166 with the predetermined increase of specified time interval supply) or the operation of any other suitable pattern.In addition, in certain embodiments, mashing pump 166 can receive feedback from the one or more sensors that are arranged in gasifier 104 or are positioned at gasifier 104 downstreams, and responds the amount of the slurry feed of described feedback regulation pumping.Shown embodiment comprises slurry feed system, and its Raw preparation system 152 is prepared the slurry feed of coal.But in other embodiments, raw material preparation system 152 can be the dry feed system that is configured to prepare dry feed., in certain embodiments, can use dry feed system but not slurry feed system.

Slurry feed and oxygen 222 are supplied to gasifier 104 via first entrance 186 at the top that is positioned at gasifier 104.Reactant and slag flow to the first outlet 188 of gasifier 104 in the direction in downstream roughly from the first entrance 186 of gasifier 104., feed slurry and vaporized chemical (for example oxygen) occur by flowing of gasifier 104 simultaneously.In addition, can there is by this flowing of gasifier 104 residence time that is less than about 3,4,5 or 6 seconds.In gasification, the service temperature of shown airflow bed gasification furnace 104 can be about 1200 DEG C to 2000 DEG C, and working pressure can be less than about 80 bar.Shown airflow bed gasification furnace 104 utilizes steam and oxygen to allow some burnings in slurry feed, to produce carbon monoxide and to release energy.These products drive the second reaction, and raw material is further converted into hydrogen and other carbonic acid gas by described the second reaction.These reactions, occurring without any focus energy system (as plasma torch system) in the situation that, therefore can be described as non-plasma mechanism of activities of the Vital energy.In other words, use conventionally the raise temperature of whole volume of gasifier 104 of the reaction of oxygen and steam, focus on the energy (for example plasma torch) and do not rely on.Therefore, gained gas is made by gasifier 104, and does not use focus energy system (as plasma torch).Gained gas can comprise carbon monoxide and the hydrogen of about 85% equal proportion, and CH ₄, HCl, HF, COS, NH ₃, HCN and H ₂s(is in the sulphur content of raw material), but may not comprise tar, condensable hydro carbons, phenols and ammonia.In non-plasma mechanism of activities of the Vital energy process, gasifier 104 also can produce refuse, as melted powder or slag 109.

The synthetic gas producing in gasifier 104 and slag can for example, flow through the first pipeline 200 in downward mode (downstream direction) from the first outlet 188 of gasifier 104 conventionally, and enter syngas cooler 154 via the second entrance 202.In certain embodiments, before gained synthetic gas/slag mixture enters syngas cooler 154, the parts of particle removal system 106 can act on gained synthetic gas/slag mixture.That is, plasma torch system 108 can be arranged at the such as downstream part of lower region 196(of gasifier 104) in, and/or be attached to the first pipeline 200.In such an embodiment, plasma torch system 108 can comprise one or more plasma torchs, and described one or more plasma torchs are configured to remove particulate matter from the fluid in the downstream of the main gasification zone of gasifier 104.Plasma torch is fusible inorganic particle, and organic granular in the gained gas products that makes to be made by gasifier 104 reacts., particle removal system 106 can act on the product of the non-plasma base mechanism of activities of the Vital energy occurring in gasifier 104.Therefore, particle removal system 106 is configured to process exclusively the powder occurring as the product of main gasification.Like this, than the system without described novel particle removal system 106, aforementioned feature can be conducive to increase carbon conversion efficiency.For example, after the non-plasma base mechanism of activities of the Vital energy in gasifier 104, keep unreacted organic granular still can further react in downstream via plasma torch system 108.

After entering syngas cooler 154, gained fluid (for example synthetic gas and slag mixture) flows through the gas passage of syngas cooler 154, and described gas passage is second internal volume 206 that passes through extending longitudinally on flow direction 224.Therefore, gained fluid enters syngas cooler 154 by the second entrance 202, and longitudinal flow is by syngas cooler 154.Synthetic gas leaves syngas cooler 154 by the second outlet 208 subsequently, and slag abandons via the 3rd outlet 212.In this way, gained fluid can with the tube contacts of syngas cooler 154, and flow through the fluid (as water 226) of described pipeline can be for cooling gained fluid in the time that it advances by syngas cooler 154.A result of this process of cooling can be and in pipeline, produces steam 228, and steam 228 can be transferred to high drum pressure subsequently for collecting and transferring to heat recovery steam generator 138(referring to Fig. 1).

Syngas cooler 154 also can comprise following mechanism at the lower region of syngas cooler 154: described mechanism can assist guiding to leave syngas cooler 154 through cooling synthetic gas and slag by outlet 208 and 212 separately.For example, slag 109 can be directed in roughly downward direction 224 and flow, to leave syngas cooler 154 via outlet 212.By contrast, can be directed to the second outlet 208 and second pipe 210 and flow through cooling synthetic gas.The slag that leaves the 3rd outlet 212 is directed to slag and removes system 156 for processing.First slag enters valve 168, and described valve 168 is controlled the amount of the slag that separates and remove via lock hopper 172.Lock hopper 172 is collected the fluid entering, and is passed to valve 170 with desired rate.Can process subsequently or use in downstream application through the slag 109 of removing.

Gained synthetic gas leaves syngas cooler 154 via the second outlet 208.In certain embodiments, synthetic gas can further be processed by particle removal system 106 after leaving syngas cooler 154.That is, as previously mentioned, particle removal system 106 can further make the reaction of any organism, and for example, via any remaining inorganics staying in the focus energy plasma beam of plasma torch (from) fusing synthetic gas, as shown in arrow 218.Unreacted synthetic gas can enter gas cleaning unit 110 subsequently for further processing.Water scrubber 174 is removed powder from synthetic gas, thereby produces the synthetic gas 176 through washing, than undressed synthetic gas, and the described pollutent that contains reducing amount through the synthetic gas 176 of washing.Synthetic gas 176 through washing can be used for gas turbine fuel, chemical manufacture etc.The stream abandoning leaves water scrubber 174.The first part of the stream abandoning processes as Heisui River 180 by valve 178.The second section of the stream abandoning is conducted through recirculation loop 182, with further clean undressed synthetic gas in water scrubber 174.

Fig. 3-5 are the block diagram of each embodiment of gasification system, and wherein focus energy system (for example plasma torch system 108) for example can be arranged at, in one or more focus energy gasifiers (plasma gasification device).Particularly, Fig. 3 shows gasification system or process 250, and it comprises raw material preparation system or process 152, gasifier 104, plasma unit 252, syngas cooler 154, powder or slag removal system or process 156, and gas cleaning unit 110.As previously mentioned, gasifier 104 comprises the first entrance 186, the first outlet 188, and limits the shell 190 of the first internal volume 192.But in this embodiment, the first outlet 188 of gasifier 104 is open in pipeline 254, described pipeline 254 is attached to the outlet of gasifier 104 188 the 3rd entrance 256 of plasma unit 252.Shell 258 limits the 3rd internal volume 260 of plasma unit 252.Pipeline 262 is attached to the 4th outlet 264 of plasma unit 252 the second entrance 202 of syngas cooler 154.As previously mentioned, syngas cooler 154 is attached to second pipe 210 by the second internal volume 206, the second outlets 208 that shell 204 limits syngas cooler 154, and syngas cooler 154 is attached to powder in the 3rd outlet 212 or slag is removed system 156.

As described in detail, in operating process, raw material preparation system 152 is prepared the slurry feed of the coal of about 50% to 70% weight in water.That is, mashing pump 166 enters the slurry feed in slurry tank 164, and the amount that is applicable to gasification 150 is passed to gasifier 104 via pipeline 220.Slurry feed and oxygen 222 are supplied to gasifier 104 via first entrance 186 at the top that is positioned at gasifier 104.Reactant and slag flow to the first outlet 188 of gasifier 104 in the direction in downstream roughly from the first entrance 186 of gasifier 104.Gasifier 104 utilizes steam and oxygen so that some in slurry feed can be burnt, to produce carbon monoxide and to release energy.Reaction is subsequently further converted to hydrogen and other carbonic acid gas via non-plasma mechanism of activities of the Vital energy by raw material.In this way, gasifier 104 is manufactured gained gas and is produced refuse (for example slag).

The synthetic gas and the slag that in gasifier 104, produce can for example, flow through pipeline 254 in downward mode (downstream direction) from the outlet 188 of gasifier 104 conventionally, and enter plasma unit 252 via entrance 256.After entering plasma unit 252, gained fluid (for example synthetic gas and slag mixture) flows through the passage of plasma unit 252, and described passage is the 3rd internal volume 260 that passes through extending longitudinally on flow direction 224.In the embodiment show in figure 3, plasma unit 252 comprises focus energy system (for example plasma torch system 108).In such an embodiment, plasma unit 252 can comprise one or more focus energy equipment (for example plasma torch), and described one or more focus energy equipment is configured to remove particulate matter from the fluid in gasifier 104 downstreams.In certain embodiments, plasma unit 252 can be plasma processing unit, as plasma gasification device.The fusible inorganic particle of focus energy equipment (for example plasma torch) in plasma unit 252, and organic granular in the gained fluid that makes to be made by gasifier 104 reacts.Therefore, particle removal system 106 is configured to the powder that gasifies exclusively and occur as the product of main gasification.Like this, keep after the non-plasma base mechanism of activities of the Vital energy in gasifier 104 unreacted organic granular still can be in plasma unit 252 at the downstream reaction of gasifier 104.In certain embodiments, non-plasma base mechanism of activities of the Vital energy can comprise air flow bed, fixed bed, fluidized-bed, ebullated bed or circulating fluidized bed.

The plasma torch that is arranged in plasma unit 252 can arrange in any mode that is applicable to process the fluid stream being produced by gasifier 104.For example, one or more plasma torchs can be attached to shell 258 with multiple setting.In certain embodiments, plasma torch can circumferentially arrange around the inwall of shell 258, and directed roughly to assemble the plasma flow of appearance toward each other.In another embodiment, plasma torch can be around the inwall of shell 258 with different angles setting, the subset construction that makes plasma flow (for example, can arrange 2,3,4,5 or multiple groups of more plasma torch, make every group of torch have the plasma flow of convergence) for assembling.In a further embodiment, one or more plasma torchs can be configured to respect to longitudinal flow by the 3rd internal volume 260 of plasma unit 252, directing plasma flow on updrift side, downstream direction or upstream and downstream direction.In fact,, in the embodiment expecting at present, one or more plasma torchs can arrange by any way in plasma unit 252.

For example, can conventionally for example, flow through pipeline 262 and enter syngas cooler 154 via the second entrance 202 in downward mode (downstream direction) via outlet 264 fluids through Cement Composite Treated by Plasma (synthetic gas and slag) that leave plasma unit 252.Gained fluid enters syngas cooler 154 by the second entrance 202, and longitudinal flow is by syngas cooler 154, is cooled in described syngas cooler 154 through the fluid of Cement Composite Treated by Plasma.As mentioned above, synthetic gas leaves syngas cooler 154 by the second outlet 208 subsequently, and slag abandons via the 3rd outlet 212.The slag that leaves the 3rd outlet 212 is directed to slag and removes system 156 with processing or for downstream application.Unreacted synthetic gas can enter gas cleaning unit 110 subsequently for further processing.As previously mentioned, gas cleaning unit 110 produces the synthetic gas 176 through washing that can be used for gas turbine fuel, chemical manufacture etc.

Fig. 4 is the block diagram of an embodiment of gasification system or process 280, it comprises that raw material preparation system or process 152, gasifier 104, syngas cooler 154, powder or slag remove system or process 156, plasma unit 252, and gas cleaning unit 110.Than Fig. 3, after plasma unit 252 is positioned at syngas cooler 154 in the fluid flow path by gasification 280.That is, in this embodiment, feed preparation unit 152 is prepared slurry feed, and described slurry feed is for example fed to gasifier 104, for main gasification (non-plasma base gasification) together with oxygen 222.But the gained fluid occurring from gasifier 104 enters immediately plasma unit 252 unlike Fig. 3, but enters syngas cooler 154 via pipeline 200.Gained fluid is cooling in syngas cooler 154 subsequently, and is separated into slag 109 and undressed synthetic gas.Undressed synthetic gas leaves syngas cooler 154 via outlet 208, and enters plasma unit 252 via entrance 256.That is, in this embodiment, only undressed synthetic gas and enter plasma unit 252 without slag 109.Plasma unit 252 can comprise one or more focus energy equipment (for example plasma torch), and described one or more focus energy equipment is configured to from undressed synthetic gas, remove particulate matter after cooling and slag are removed.The fusible inorganic particle of focus energy equipment in plasma unit 252, and make to be held in the organic granular reaction in undressed synthetic gas.The undressed synthetic gas of for example, processing through high energy (plasma body) that leaves plasma unit 252 via outlet 264 enters gas cleaning unit 110, and gas cleaning unit 110 produces the synthetic gas 176 through washing.

Fig. 5 is the block diagram in the downstream of gasifier 104 with the gasification system of plasma unit 252 or another embodiment of process 290.In this embodiment, gasification system 290 comprises raw material preparation system or process 152, gasifier 104, syngas cooler 154, powder or slag removal system or process 156, and gas cleaning unit 110.But than the embodiment of Fig. 2-4, plasma unit 252 is arranged in gas cleaning unit 110 or associated with gas cleaning unit 110.Therefore the undressed synthetic gas, occurring from the outlet 208 of syngas cooler 154 is passed to gas cleaning unit 110.As previously mentioned, undressed synthetic gas is passed to water scrubber 174, and described water scrubber 174 is removed powder, produces thus the synthetic gas 176 through washing.In certain embodiments, the powder of removal can be used in plasma unit 252, for example, with the organic granular reaction in the powder (filter cake) that melts inorganic particle and make to remove, as further discussed in detail.Synthetic gas 176 through washing can be used for gas turbine fuel, chemical manufacture etc.The stream abandoning leaves water scrubber 174.A part for the stream abandoning is conducted through recirculation loop 182, with further clean in water scrubber 174.Another part of the stream abandoning is processed as Heisui River 180 by valve 178.

In the embodiment shown in fig. 5, plasma unit 252 can be configured to receive Heisui River 180 by entrance 256, and via plasma-based gasification process Heisui River 180, for example, and/or plasma unit 252 can be configured to receive filter cake (filtering out the powder in Heisui River) by entrance 256, and make filter cake reaction via one or more plasma flows or plasma sheet.That is, in the embodiment of expection at present, for example plasma unit 252 of particle removal system 106() can be attached to waste pipe or treatment unit for waste water, or system 106 can be attached to removal particle pipeline or delivery system.The Cement Composite Treated by Plasma in Heisui River 180 can make any organic granular reaction in Heisui River and form byproduct gas.Can trap, cooling and clean described byproduct gas is for use or processing subsequently.In addition, the inorganic particle in Heisui River 180 is fusible, and forms liquid silicon hydrochlorate in the bottom of plasma unit 252.Liquid silicon hydrochlorate can be passed to shrend from plasma unit 252, and liquid silicon hydrochlorate is condensed into solid silicate for processing in shrend place.Equally, the Cement Composite Treated by Plasma of filter cake also can produce byproduct gas from any unreacted carbon that may be held in filter cake.

It should be noted that plasma unit 252 shown in this article can be applicable to shown in the gasifier of any type in gasification system.For example, suitable gasifier can use plasma body and pressing down gasification feed in oxygen environment, and can slightly under negative pressure, operate.Further for example, in certain embodiments, plasma unit 252 can be fixed bed gasifiers.In such an embodiment, plasma gasification can occur at the temperature of about 2000 DEG C to 5000 DEG C, and byproduct gas can be left plasma unit 252 at the temperature of about 700 DEG C to 1500 DEG C.Further for example, plasma unit 252 can be fluidized-bed gasifier.In these embodiments, plasma reaction district can have the temperature that is less than about 2000 DEG C to 5000 DEG C.

Fig. 6 shows the gasification system of an exemplary plasma system 108 or the block diagram of process 300.Gasification system 300 comprises the gasifier 104, pipeline 200, plasma system 108, syngas cooler 154, powder or the slag removal system 156 that are configured to receive fuel 101 and oxygen 222, and gas cleaning unit 110.In operating process, fuel 101 and oxygen 222 enter gasifier 104 via entrance 186.Gasifier 104 utilizes oxygen, via the gasification of non-plasma base, fuel is converted into gained gas and refuse (for example slag).Gained fluid (for example gas and refuse) leaves gasifier 104 via outlet 188, and enters pipeline 200.Gained fluid is advanced by pipeline 200 along the path being represented by arrow 302 on downstream direction.Focus energy system (for example plasma system 108) is configured to the longitudinal axis guided focused energy flow (for example plasma flow) in the upstream direction along pipeline 200, as shown in arrow 204.In this way, the updrift side of focus energy stream (for example plasma flow 304) is relative with the downstream direction of fluid stream 302, and fluid stream 302 is assembled with plasma flow 304 in pipeline 200.That is, plasma system 108 is set to directing plasma flow 304 in a first direction, and described first direction is conventionally relative with the second direction of fluid stream 302.For example, in the embodiment shown, the angle between first direction and second direction is about 180 degree.In a further embodiment, the first and second directions can be orientated with the angle relative to each other that is less than about 5,10,15,20,30 or 40 degree.For example, first direction can be along longitudinal axis setting, and second direction can be with the angle setting of spending from the longitudinal axis 10.Further for example, first direction can be with the angle setting of spending from the longitudinal axis 5, and second direction can be with the angle setting of spending from the longitudinal axis 10.Therefore, in such an embodiment, plasma flow 304 interacts with fluid stream 302, thereby makes organic granular reaction, and fusing is contained in the inorganic particle in fluid stream 302.

After interacting with plasma flow 304, fluid 306 through Cement Composite Treated by Plasma enters syngas cooler 154 by the second entrance 202, and longitudinal flow is by syngas cooler 154, is cooled in described syngas cooler 154 through the fluid of Cement Composite Treated by Plasma.As mentioned above, synthetic gas leaves syngas cooler 154 by the second outlet 208 subsequently, and slag abandons via the 3rd outlet 212.The slag that leaves the 3rd outlet 212 is directed to slag and removes system 156 with processing or for downstream application.Unreacted synthetic gas can enter gas cleaning unit 110 subsequently for further processing.As previously mentioned, gas cleaning unit 110 produces the synthetic gas 176 through washing that can be used for gas turbine fuel, chemical manufacture etc.

Fig. 7 is the cross-sectional side view of the bottom section (for example downstream part) of exemplary plasma unit 252.In the embodiment shown, plasma torch system 108 comprises plasma unit 252, multiple plasma torch 320,322,324,326,328,330 and 332, and controlling plasma device 334.Multiple plasma torchs different axially, radially and/or circumferential position place around the wall setting of shell 258.For example, plasma torch 320 and 332 is arranged at the first axial location, and torch 322 and 330 is arranged at the second axial location, and torch 324 and 328 is arranged at the 3rd axial location, and torch 326 is arranged at the four-axial position (for example bottom) of plasma unit 252.In addition, plasma torch 332 is to arrange with respect to plasma torch 330 first angles 336, and plasma torch 328 is to arrange with respect to plasma torch 330 second angles 338.Similarly, plasma torch 320 is to arrange with respect to plasma torch 322 first angles 336, and plasma torch 324 is to arrange with respect to plasma torch 322 second angles 338.In the embodiment shown, plasma torch 322 for example, arranges in the horizontal plane of (for example, perpendicular to fluid stream) intersecting with the longitudinal axis of plasma unit 252 (vertical) with 330.Therefore, the first angle 336 is directed to downstream, and the second angle 338 is directed to upstream.The first angle 336 and the second angle 338 can be between 1 to 90 degree, between 5 to 80 degree, between 10 to 70 degree, between 20 to 60 degree, between 30 to 50 degree, or approximately 45 degree.In addition, the first angle 336 and the second angle 338 can be same to each other or different to each other.In a further embodiment, the first angle 336 and the second angle 338 are variable in operating process.That is, in operating process, the angle of each in plasma torch can change, to adapt to the change of operational condition, performance etc.For example, in one embodiment, the first angle 336 can change, and makes plasma torch 332 with the angle guiding stream 352 perpendicular to stream 354.It is 354 relative that plasma torch 326 and fluid flow.

The aforementioned setting of plasma torch can have following effect: the central area that multiple plasma flows 340,342,344,346,348,350 and 352 are converged in plasma unit 252 toward each other., multiple plasma torchs are set to guide toward each other multiple plasma flows.In the embodiment shown, seven plasma flows are assembled.But, in alternative embodiment, the plasma torch of any amount can be set, the plasma flow of any amount is assembled.For example, the quantity of converging streams can be about 2 to 10,5 to 20 or any other suitable quantity.Further for example, the quantity of converging streams can be at least about 3,4 or 5.Also it should be noted that multiple plasma torchs can have multiple setting in shell 258.Although Fig. 7 only shows 7 plasma torchs, plasma torch system 108 can comprise the plasma torch of any amount, for example 1 to 10,1 to 50 or 1 to 100.In addition characteristic (for example size of plasma unit 252 or capacity) that, can be based on plasma unit 252 and select the spacing between plasma torch.For example, plasma torch can be at the interior even or non-uniform spacing of shell 258.As shown, plasma unit 252 supports plasma torch in shell 258 evenly to arrange.But the distance between adjacent plasma torch can be equidistant, or can between plasma torch, change.In addition, although illustrated embodiment has shown the plasma torch in plasma torch system 108, can for example, in focus energy system (plasma torch system 108), use any suitable setting of the focus energy equipment (for example plasma torch) of any type.

In operating process, fluid stream 354 for example, is set up towards plasma torch 326 (relative direction) on downstream direction roughly.In the time that fluid stream 354 is longitudinally advanced by plasma unit 252, multiple plasma flows converge on stream 354, and interact with the content of fluid.For example, the fusible inorganic particle being contained in fluid of energy of plasma.Further for example, energy of plasma can make organic granular (as the resistates from the non-plasma base gasification) reaction in fluid.Again, comprise that this plasma-based gasification step can have the carbon conversion efficiency that increases total gasification system, because keep unreacted carbonaceous material still can react in plasma-based gasification after the gasification of non-plasma base.

In the embodiment shown, controlling plasma device 334 is configured to control independently the plasma flow relevant to plasma torch 320,322,324,326,328,330 and 332.Feedback that, controlling plasma device 334 can be based on from sensing system, baseline parameter, predetermined limit, historical data etc. are controlled the performance characteristic of the multiple plasma torchs in plasma torch system 108.For example, controlling plasma device 334 can be configured to characteristic (as volume, flow velocity, the viscosity etc.) activation based on stream 354 or each of stopping using in multiple plasma torchs.Controlling plasma device 334 also can be configured to change the first angle 336 and/or the second angle 338 based on flow characteristics.Further for example, controlling plasma device 334 can with the sensing system binding operation of measuring stream 354 characteristic, and can be depending on received feedback and use closed-loop control, thereby change the activity of plasma torch with even mode or non-homogeneous mode.For example, if sensor system senses to the rate reduction of the stream 354 by plasma unit 252, one or more to adapt to the minimizing of fluid in can activate plasma torch of controlling plasma device 334.Similarly, if stream 354 speed increases, one or more so that adapt to must be by the fluid load of the increase of energy of plasma processing in can activate plasma torch of controlling plasma device 334.Even further for example, controlling plasma device 334 can be controlled the performance characteristic of plasma torch, as temperature, energy/volume etc.In such an embodiment, can use sensor, described sensor detects the amount of the unreacted organic granular in the gas stream leaving, and adjustment operation characteristic correspondingly.For example, controlling plasma device 334 adjustable-angles 336 and/or 338, for example, to be conducive to better mixing by producing plasma plume (extensive whirlpool).

Fig. 8 is the cross-sectional view of the plasma unit 252 that obtains along the line 8-8 of Fig. 7, and it shows the single axial location in plasma unit 252.As shown, plasma unit 252 comprises plasma torch 322, plasma torch 330, plasma torch 370 and plasma torch 372., the circumference of plasma torch 322,330,370 and 372 walls around shell 258 arranges at different positions place.The described circumferential setting of plasma torch can have following effect: make multiple plasma flows 342,350,374 and 376 converge at toward each other center-diameter in plasma unit 252 to location.In the embodiment shown, four plasma flows are assembled.But, in alternative embodiment, the plasma torch of any amount can be set, the plasma flow of any amount can be assembled.For example, the quantity of converging streams can be at least about 3,4 or 5.Also it should be noted that multiple plasma torchs can have multiple setting in any radial position place in shell 258.Although Fig. 8 only shows 4 plasma torchs, plasma torch system 108 can be included in the plasma torch of any amount that arbitrary axial positions arranges, for example 1 to 10,1 to 50 or 1 to 100.In addition, plasma torch can be around the even circumferential of shell 258 or non-uniform spacing.That is, the distance between adjacent plasma torch can be equidistant, or can between plasma torch, change.Can be in any suitable setting of axial positions use plasma torch arbitrarily in plasma torch system 108.In addition,, although illustrated embodiment has shown the plasma torch in plasma torch system 108, can in focus energy system, use any suitable setting of the focus energy equipment of any type.

Fig. 9 is the cross-sectional view of an alternative exemplary embodiment of the plasma unit 252 that obtains along the line 8-8 of Fig. 7.In this embodiment, multiple plasma torchs 322,330,370 and 372 are configured to produce multiple plasma sheets 390,392,394 and 396.,, in operating process, plasma torch 322 produces from plasma torch 322 and outwards departs from the plasma sheet 390 that enters interior chamber 260.Similarly, plasma torch 370 produces the plasma sheet 392 outwards departing from from torch 370, and plasma torch 330 produces the plasma sheet 394 outwards departing from from torch 330, and plasma torch 372 produces the plasma sheet 396 outwards departing from from torch 372.These plasma sheets 390,392,394 and 396 can, in common plane, to increase the coverage in plasma unit 252, make the more fluid/particle reaction in stream thus.Aforementioned feature can have following effect: make plasma sheet converge at the central area in chamber 260.Be contained in energy of plasma and the Interaction between particles being contained in flowing by the fluid of plasma unit 252 in this.That is, as previously mentioned, plasma sheet 390,392,394 and 396 is configured to melt inorganic particle, and makes the organic granular reaction in fluid stream.As previously mentioned, although illustrated embodiment has shown the plasma torch in plasma unit 252, can in focus energy system, use any suitable setting of the focus energy equipment of any type.

In certain embodiments, utilize the powder treatment system of above-mentioned plasma gasification device to can be used for the waste streams that processing produces from the gasification of the first fuel feedstocks.Referring now to Figure 10, an example of the IGCC system 100 that comprises powder treatment system is described.Gasification system 100 comprises and can receive for example the first fuel feedstocks of fuel 101(by feed preparation unit 102) gasifier 104, gas cleaning unit 110, black water treatment system 402, Powdex filter 404 and powder treatment system 406.Although powder treatment system 406 can be used together with IGCC system 100, powder treatment system 406 also can be used for using or producing in any person in polytype factory of synthetic gas.For example, powder treatment system 406 can be used in any factory of generation CO as above, hydrogen, methyl alcohol, ammonia or any other chemistry or fuel product.In addition, in certain embodiments, can use the powder treatment system 406 of unpowered generation (for example generator).

Described above about Fig. 1, solid fuel 101 can be passed to feed preparation unit 102, gasification in gasifier 104, and the clean synthetic gas producing in gas cleaning unit 110 afterwards, to produce treated synthetic gas.The waste streams producing in gas cleaning unit 110 is passed to usage on black water unit 402, and filters by Powdex filter 404, produces buck 438 with separated powder from Heisui River 436.In certain embodiments, Powdex filter can trap about 90-100% of powder particle, and wherein about 20-60% of powder is less than 50 microns.Therefore, powder forms the filter cake 405 of the solid material of the water that contains about 20-60% and 40-80%.Gained filter cake 405 can have the unreacted carbon of significant quantity, and described unreacted carbon can for example use one or more high fluence or sheet via powder treatment system 406(, as the plasma body in focus energy system 408) and be converted into the second synthetic gas 409.Synthetic gas 409 then can be used for producing equipment 410(as firing system, engine, turbine etc. for power) power is provided.Than the gasification of the first fuel feedstocks by gasifier 104 and the synthetic gas producing, the second synthetic gas can have different compositions.This may be caused by following: than the first fuel feedstocks, and the inorganic materials of the increasing amount in filter cake 405.In another embodiment, waste streams can comprise from the refuse of adjacent factory and/or biomass waste (as timber or garden refuse), or any combustible matl of sulfur-bearing not, or their combination.The gasification that it should be noted that the filter cake 405 in powder treatment system 406 also produces slag 412, described slag 412 can be in slag treatment unit 416 with gasifier 104 in the slag 109 that produces combine.As discussed above, slag 109 and 412 can be processed, and as for example roadbase or material of construction.In a further embodiment, controller 420 can be attached to gasifier 104 and powder treatment system 406, to control independently and side by side gasifier 104 and powder treatment system 406, as described in detail.

Powder treatment system 406 comprises for example plasma torch system of focus energy system 408().Figure 11 is the block diagram that comprises the region 430 of the IGCC system 100 of the powder treatment unit 406 with focus energy system 408.Region 430 can be positioned at the downstream of gas cleaning unit 110, makes powder treatment system 406 to receive waste streams by inlet valve 432.In one embodiment, the focus energy system 408 of powder treatment system 406 comprises the plasma gasification device 440 with plasma torch system 442.Plasma torch system 442 can provide high-energy focusing bundle (for example plasma flow and/or sheet) to melt inorganic component, and makes the organic constituent reaction existing in filter cake 405.Filter cake 405 can comprise from the powder of material gasification or coal smoke.In certain embodiments, plasma torch system 442 can comprise one or more plasma torchs 443, and described one or more plasma torchs 443 produce the plasma body 445 that is applicable to gasification.For example, plasma torch 443 can comprise for received current and produce two electrodes of electric arc.Such as, in the time of rare gas element (nitrogen, argon gas etc.) process electric arc, plasma torch 443 can be retained to the internal temperature of much approximately 5000 DEG C.For example, the internal temperature in plasma torch 443 can at least be greater than about 2000 DEG C, 3000 DEG C, 4000 DEG C or 5000 DEG C.

Plasma gasification device 440 shown in this article can be applicable to shown in the gasifier of any type in gasification system, and plasma gasification device 440 can have about internal volume of 2.5%, 5%, 7.5%, 10%, 12.5% or 15% of the internal volume that is at least less than gasifier 104.In one embodiment, plasma gasification device 440 can be fixed bed gasifiers.Therefore, gasification can occur at the temperature between about 2000 ° to 5000 DEG C.In another embodiment, plasma gasification device 440 can be following gasifier: its unreacted carbon in filter cake 405 that can gasify in anaerobic environment, and can slightly under negative pressure, operate.In another embodiment, plasma gasification device 440 can comprise fluidized-bed gasifier.Like this, the gasification of filter cake 405 can occur at the temperature that is less than about 2000 DEG C to 5000 DEG C.

After filter cake 405 gasifies in plasma gasification device 440, as the second undressed synthetic gas 409(, it for example can remain on, under low pressure (environmental stress) gained the second synthetic gas 409) leave by outlet valve 434, and in synthetic gas processing unit 448, process to remove any undesirable material producing in gasification, thereby produce the treated synthetic gas 450 of low pressure second.In one embodiment, synthetic gas processing unit 448 can comprise washer, and described washer is such as but not limited to sulfur scrubber unit.In another embodiment, synthetic gas processing unit 448 can use liquid-phase oxidation process (can derive from the Sweet natural gas technical products company (Gas Technology Products LLC Corporation ofHouston, TX) of Houston, Texas liquid oxidation reduction), to remove sulphur from undressed synthetic gas.The second treated synthetic gas 450 can be used for providing power for power produces equipment 410, and described power produces the oil engine that equipment 410 can comprise internal combustion turbine, have reciprocating piston, or another aerodynamic force engine.For example, in one embodiment, power produces equipment 410 and can be Jenbacher reciprocating combustion gas engine, or the engine of the other types that provided by the General Electric Corporation (General Electric Company of Schenectady, N.Y) of Schenectady, New York.Jenbacher engine (or other equipment 410) low pressure that are suitable for burning (for example environmental stress) fuel, as the synthetic gas that can produce from plasma gasification device 440.For example, engine can comprise there is 1 to 30, the oil engine of 4 to 20 or 8 to 16 cylinders and relevant reciprocating piston.In another embodiment, power produces equipment 410 and can be vapour generator.In another embodiment, the synthetic gas combination that the second treated synthetic gas can produce with the first fuel feedstocks from gasifier 104.Depend on and how to use, the second treated synthetic gas 450 is compressible or do not compress.

In an embodiment of the present disclosure, the information providing via input signal 462 can be provided controller 420, to carry out the instruction or the coding that are contained on mechanical-readable or computer-readable recording medium, and produce the one or more output signals 460 that arrive various operating devices (as control valve or pump).For example, based on being contained in instruction on mechanical-readable or the computer-readable medium of controller 420 or the execution of coding, output signal 460 can be used for controlling the gasification of the first fuel feedstocks 102 and waste streams (for example filter cake 405).Especially, the instruction of execution can be indicated gasification the first fuel feedstocks 102, purified synthesis gas, filtration waste streams (for example Heisui River 436), and in plasma gasification device 440, processes filter cake 405 to produce the second synthetic gas 409.In certain embodiments, temperature sensor 452 and/or pressure transmitter 456 can be sent to controller 420 by input signal 462, thereby indicate respectively temperature and/or the pressure of plasma gasification device 440.Therefore,, if the temperature of instruction or pressure exceed the limit of plasma gasification device 440, controller 420 can transmit output signal 460 to cut out plasma gasification device 440 or to activate safety trip.In another embodiment, operator can provide instruction to controller 420, thereby so that obtains the mode operation IGCC system 100 that the efficiency of carbon conversion of the first fuel feedstocks 102 in gasifier 104 reduces.For example, the gasification of the limit oxygen environment of the first fuel feedstocks 102 can produce the unconverted carbon of the increasing amount in filter cake 446.The unconverted carbon of the gasifiable gasification from the first fuel feedstocks 102 in filter cake 446 of plasma gasification device 440, therefore, can keep the carbon conversion efficiency of IGCC system 100.

Technique effect of the present invention comprises the powder treatment system 406 that comprises focus energy system (for example plasma torch system 442) that uses, and described focus energy system is processed the waste streams (for example filter cake 405) producing in IGCC gasification system 100.The unreacted carbon that gasification waste streams contains significant quantity, described unreacted carbon can be converted into synthetic gas.Like this, carbon conversion efficiency can be increased, and the needs of processing or reclaiming gained waste streams can be significantly reduced or eliminated.The synthetic gas producing is clean in synthetic gas processing unit 448, and is used to power to produce equipment 410(as Jenbacher engine or vapour generator) power is provided.In addition, the enforcement of powder treatment system 406 allows the operator of IGCC gasification system with the lower mode operation factory of the efficiency of carbon conversion in gasifier 104, because powder treatment system 406 can transform remaining unreacted carbon.

This written description is used the example that comprises best mode with open the present invention, and makes any those skilled in the art can implement the present invention, comprises the method for manufacturing and using any device or system and carry out any introducing.The scope of the claims of the present invention is defined by the claims, and can comprise other examples that those skilled in the art expect.If other examples have not different from the word language of claims structural elements, if or other examples comprise the equivalent structure element with the word language of claims with unsubstantiality difference, other such examples are intended to fall in the scope of claims.

Claims

1. a system, it comprises:

Gasifier, described gasifier comprise there is the first entrance, the first outlet and the first shell of the first internal volume, wherein said the first entrance is configured to receive the first fuel feedstocks and enters described the first internal volume, and described the first exit structure is for to export the first synthetic gas from described the first internal volume; And

Plasma gasification device, described plasma gasification device is arranged at the downstream of described the first outlet, and is attached to the waste streams producing from described the first fuel feedstocks by gasifier.

2. system according to claim 1, is characterized in that, described plasma gasification device comprise there is the second entrance, the second outlet and second housing of the second internal volume, wherein multiple plasma torchs are attached to described second housing.

3. system according to claim 2, is characterized in that, described the second internal volume is at least less than about 5% of described the first internal volume.

4. system according to claim 2, is characterized in that, described multiple plasma torchs are directed roughly to assemble plasma flow toward each other.

5. system according to claim 1, is characterized in that, described waste streams comprises filter cake, and described filter cake is made by the Hei Shuiyuan that filters the Powdex filter unit by being communicated with described plasma gasification device fluid.

6. system according to claim 5, is characterized in that, described plasma gasification device comprises the second entrance, and described the second entrance is configured to receive the described filter cake from described Powdex filter.

7. system according to claim 5, is characterized in that, described filter cake processes to produce the second synthetic gas in described plasma gasification device.

8. system according to claim 7, is characterized in that, plasma gasification device is configured to described the second synthetic gas to pass through the second outlet.

9. system according to claim 7, it comprises that power produces equipment, described power generation equipment is configured to receive described the second synthetic gas to produce power.

10. system according to claim 9, is characterized in that, described power generation equipment comprises internal combustion turbine, oil engine or steam turbine.

11. 1 kinds of methods, it comprises:

First fuel feedstocks that gasifies in gasifier, to produce the first synthetic gas and waste streams;

Filter described waste streams, to produce the second fuel feedstocks; And

In plasma gasification device, process described the second fuel feedstocks, to produce the second synthetic gas.

12. methods according to claim 11, is characterized in that, described the first fuel feedstocks comprises coal, oil or biomass, or their combination.

13. methods according to claim 11, is characterized in that, described plasma gasification device comprises the second entrance, the second outlet, the second internal volume and multiple plasma torch.

14. methods according to claim 11, is characterized in that, described the second fuel feedstocks comprises filter cake.

15. methods according to claim 14, is characterized in that, described filter cake is passed to described plasma gasification device by the second entrance, and process with multiple plasma torchs, to produce described the second synthetic gas.

16. methods according to claim 11, it comprises described the second synthetic gas is passed to synthetic gas processing unit.

17. methods according to claim 11, it is included in described the second synthetic gas that burns in firing system.

18. 1 kinds of systems, it comprises:

Be arranged at the instruction on nonvolatile machine readable media, wherein said instruction is configured to:

First fuel feedstocks that gasifies in gasifier, to produce the first synthetic gas and waste streams; And

In plasma gasification device, process the filter cake from described waste streams, to produce the second synthetic gas.

19. systems according to claim 18, it comprises the controller with described instruction.

20. systems according to claim 18, is characterized in that, described instruction is configured to control the operation in integrated gasification combined cycle plants (IGCC) power station that comprises two or more gasifiers.