CN103402911A

CN103402911A - Systems and methods for maintaining sulfur concentration in a syngas to reduce metal dusting in downstream components

Info

Publication number: CN103402911A
Application number: CN2011800687418A
Authority: CN
Inventors: J·阿布哈泽尔赫
Original assignee: Kellogg Brown and Root LLC
Current assignee: Kellogg Brown and Root LLC
Priority date: 2010-12-30
Filing date: 2011-12-06
Publication date: 2013-11-20
Also published as: WO2012091856A1; US20120167466A1

Abstract

Systems and methods for maintaining a sulfur concentration in a syngas are provided. The method can include combining sulfur and a carbonaceous material to produce a sulfur containing carbonaceous feed. The method can also include gasifying at least a portion of the sulfur containing carbonaceous feed to produce a syngas and detecting a sulfur concentration in the syngas. The method can further include adjusting an amount of the sulfur combined with the carbonaceous material based on the detected sulfur concentration.

Description

Be used for keeping the sulphur concentration of synthetic gas to reduce the system and method for metal dusting in downstream components

The cross reference of related application

The application requires the right of priority of No. 12/982523 U.S. Patent application of submitting on December 30th, 2010, at this, is introduced into as a reference.

Background

The embodiment of describing relates generally to the system and method for the production of synthesis gas.More specifically, this kind embodiment relates to for the sulphur concentration that keeps synthetic gas to reduce the system and method for metal dusting in downstream components.

Description of Related Art

Gasifier has produced synthesis gas (synthesis gas) or " synthetic gas (syngas) " and this synthetic gas and can be further processed in downstream.Owing to synthetic gas, interacting, particularly at high temperature with synthetic gas, interact, by metal for example the downstream components that forms of heat transfer tube can suffer metal dusting, also be referred to as carburizing.Term " metal dusting " refers to metal to be fragmented into severe and the aggressiveness corrosion of dust or powder.

Several different methods is for reducing inducement and/or the impact of metal dusting.A kind of method is the alloy of selecting for the metal dusting resistant of downstream components.Another kind method is to come assembly downstream to apply coating with making metal dusting be reduced to minimum coated material.Yet these two kinds of methods need to be carried out the assembly that uses in existing gasifier system expensive change and/or be substituted.

Sulphur is the known inhibitor of metal dusting.Sulphur can be absorbed on metallic surface and stop the transfer of carbon from gas to the metal.The typical feed of gasifier comprises sulphur, and described charging for example or carbon raw material.Yet the sulphur level in these gasifier feed may be lower than the minimum level that reduces or stop the needed sulphur of metal dustingization.

Therefore, need to be for the production of synthetic gas, and sulphur concentration is enough to reduce the system and method for the metal dusting in the gasifier downstream components.

The accompanying drawing summary

Fig. 1 has described according to described one or more embodiments, and for the production of the schematic diagram of the illustrative gasification system of synthetic gas, the concentration of described synthetic gas is enough to reduce the metal dusting in the downstream components of one or more gasifiers.

Fig. 2 has described according to described one or more embodiments, and for the production of the schematic diagram of another illustrative gasification system of synthetic gas, the concentration of described synthetic gas is enough to reduce the metal dusting in the downstream components of one or more gasifiers.

Describe in detail

The system and method that is used for keeping the synthetic gas sulphur concentration is provided.Described method can comprise sulphur and carbonaceous material are made up to generate the carbonaceous feed that comprises sulphur.Described method can also comprise that at least a portion that makes the carbonaceous feed that comprises sulphur gasifies to generate synthetic gas and detects sulphur concentration in synthetic gas.Described method also comprises based on the sulphur concentration that detects, and regulates the amount of the sulphur that makes up with carbonaceous material.

Fig. 1 has described according to one or more embodiments, generates the schematic diagram of the illustrative gasification system 100 of synthetic gas through pipeline 151, and the sulphur concentration of described synthetic gas is enough to reduce the metal dusting in gasifier 150 downstream components.Gasification system 100 can comprise that one or more locking hoppers or storage hopper 110,130 are used to one or more gasifier feed system 140 chargings, and wherein said gasifier feed can store or process entering one or more gasifiers 150 before generating synthetic gas.Elemental sulfur can be stored in one or more " first " locking hoppers or storage hopper 110, described locking hopper or storage hopper can be any parts that are suitable for keeping and/or distributing sulphur.One or more feeders 120 can be assigned to raw material that one or more " second " locking hoppers or storage hopper 130 be used for storing gasification with sulphur and material combination through pipeline 122 with the sulphur from the first locking hopper 110.

Although show, feeder 120 can be fitted on the sulphur content from the first locking hopper 110 on conveyer and/or in conveyer, and conveyer can transport sulphur (transport) or transportation (convey) subsequently to the second locking hopper 130.For example, described conveyer can be travelling belt, slide plate (slide), skewed slot (chute), inclined-plane (incline) or their combination.Described conveyer can further be controlled the speed of the sulphur that is assigned to the second locking hopper 130.For example, if conveyer is travelling belt, speed that can accommodation zone to be slowly or rapidly to distribute sulphur, and the amount of the sulphur of for example measuring according to the farther place of system is regulated.

The second locking hopper 130 can receive, storage and/or mixing raw material and sulphur, in order to can obtain therein to comprise the carbonaceous material of sulphur.The second hopper 130 can will comprise the carbonaceous material transportation of sulphur or be assigned to gasifier feed system 140 through pipeline 131.Preferably, the described carbonaceous material that comprises sulphur can be transported to gasifier feed system 140 by the second locking hopper 130 through pipeline 131, the speed of described transportation is at least 50 kilograms per hour (kg/h), and more preferably, the speed of described transportation is approximately 75kg/h, approximately 100kg/h or about approximately 450kg/h, approximately 500kg/h or about 550kg/h of the paramount limit of 125kg/h of lower bound.The second locking hopper 130 can comprise the feeder (not shown), high-voltage rotary feeder for example, described feeder can coordinate with the stream (not shown) of the fluid that adds and pass through pipeline 131 with the carbonaceous material that will comprise sulphur and be transported to gasifier feed system 140.

As used in this article, term " raw material (feedstock) " refers to one or more carbonaceous materials, no matter is solid, gas, liquid or their arbitrary combination.Described raw material can comprise one or more carbonaceous materials (being carbonaceous material), described carbonaceous material includes but not limited to: biomass (namely, plant and/or animal substance or derive from plant and/or the material of animal), coal (that is, high sodium and low sodium brown coal, brown coal, sub-bituminous coal and/or hard coal), resinous shale, coke, tar, bituminous matter, low ash content or ashless minute polymkeric substance, alkyl macromolecular material, the material of biomass derived, the by product that derives from manufacturing operation or their arbitrary combination.Described alkyl macromolecular material can include but not limited to: thermoplastics, elastomerics, rubber, comprise polypropylene, polyethylene, polystyrene, comprise other polyolefine, homopolymer, multipolymer, segmented copolymer, PET(polyethylene terephthalate), poyblend, oxygen containing poly-hydrocarbon, heavy hydrocarbon mud and from the bottom product of refinery and petroleum chemical plant, chloroflo for example, its blend, its derivative or their arbitrary combination.

Described raw material can comprise two or more low ash contents or ashless minute polymkeric substance, authigenic material material or derive from mixture or the combination of the by product of manufacturing operation.For example, described raw material can comprise one or more carbonaceous materials of the consuming product combination that abandons with one or more, and the described consuming product that abandon are carpet and/or automotive plastic part/assembly for example, as collision bumper or panel board.In case of necessity, can reduce the size of these consuming product that abandon, for example before by gasification system 100, processing or pulverize in treating processes.Described raw material can also comprise the plastics of one or more recirculation, for example polypropylene, polyethylene, polystyrene, its derivative, its blend or its arbitrary combination.Therefore, gasification system 100 can be used for adjusting order, the suitable processing of the material of before making.

Through before pipeline 101 is incorporated into raw material the second locking hopper 130, can be with raw material drying, and then by one or more pulverizing mills (milling units) (not shown), pulverize.For example, can limit approximately 35% moisture drying to about 18% the moisture of lower bound by height through the raw material of pipeline 101.For example, can carry out dry raw material through pipeline 101 with the fluidized bed dryer (not shown).

Can be approximately 1 micron of lower bound, approximately 10 microns, approximately 50 microns, approximately 100 microns, approximately 150 microns or approximately approximately 1,350 micron of 200 microns paramount limit, approximately 00 micron of Isosorbide-5-Nitrae, approximately 50 microns of Isosorbide-5-Nitraes or approximately 1,500 micron through the mean particle size of the raw material of pipeline 101.For example, through the mean particle size of the raw material of pipeline 101 can for approximately 75 microns to about 75 microns of Isosorbide-5-Nitraes, approximately 125 microns to about 25 microns of Isosorbide-5-Nitraes or approximately 175 microns to approximately 1,375 micron.In another example, can be ground into mean particle size through the raw material of pipeline 101 is approximately 300 microns or less.

Thereby gasifier feed system 140 can receive the carbonaceous material that comprises sulphur through pipeline 131 and generate the first charging or " gasifier " charging through pipeline 141.Gasifier feed system 140 can will comprise the carbonaceous material of sulphur or the in check stream of carbonaceous feed is provided in gasifier 150 through line 141, the pressure change in simultaneous adaptation gasifier 150.Gasifier feed system 140 can comprise one or more locking containers or storage hopper, one or more distribution container and/or the one or more feeder that connects by one or more valves.

Alternatively, can walk around the second locking hopper 130, directly add sulphur to gasifier feed system 140 through pipeline 123.In another example, the sulphur through pipeline 124 can be added to the gasifier feed in pipeline 141, rather than add the sulphur through pipeline 121 to the second locking hopper 130 or gasifier feed system 140.In another example, the gasifier feed that can add the sulphur through pipeline 124 to pipeline 141, and the sulphur through pipeline 121 is added to the second locking hopper 130 and/or adds the sulphur through pipeline 123 to gasifier feed system 140.Although show, before the gasifier feed that is incorporated into pipeline 141 and/or gasifier 150, the sulphur that adds through pipeline 124 can be forced into the pressure of gasifier feed of pipeline 141 and/or the pressure of gasifier 150.

Can be approximately 1 micron of lower bound, approximately 10 microns, approximately 50 microns, approximately 100 microns or about approximately 400 microns, approximately 450 microns or approximately 500 microns of 150 microns paramount limits through the mean particle size of the gasifier feed of pipeline 141.For example, the mean particle size of the gasifier raw material of process pipeline 141 can be approximately 75 microns to approximately 475 microns, approximately 125 microns to approximately 425 microns or approximately 250 microns to approximately 350 microns.

Gasifier feed through pipeline 141 be directed in one or more gasifiers 150 to produce the crude synthesis gas stream through pipeline 151.Gasifier 150 can gasify at least a portion of the gasifier feed through pipeline 141 introducings to produce the crude synthesis gas stream through pipeline 151.Can be dry feed or can be used as slurry or suspension is transported to gasifier 150 through the gasifier feed of pipeline 141.Gasifier feed in pipeline 141 or the sulphur concentration that comprises the carbonaceous material of sulphur can be enough to generate the synthetic gas through pipeline 151, and described synthetic gas can reduce or prevent metal dusting in downstream processing equipment.For example, can be for being enough to generate the amount through the crude synthesis gas of pipeline 151 through sulphur concentration in the gasifier of pipeline 141 chargings, the sulphur concentration that described crude synthesis gas has is per-cent meter (vol%) at least 0.1 by volume, 0.2vol% or 0.3vol% at least at least.In pipeline 151, the sulphur concentration of crude synthesis gas can change according to the amount of adding the sulphur in the second locking hopper 130, gasifier feed system 140 and/or the process gasifier feed of pipeline 141 at least in part.For example, in pipeline 151, the sulphur concentration of crude synthesis gas can be about 0.01vol% or more, approximately 0.05vol% or more, approximately 0.1vol% or more, approximately 0.15vol% or more, approximately 0.2vol% or more, approximately 0.25vol% or more, approximately 0.3vol% or more, approximately 0.35vol% or more, approximately 0.4vol% or more, approximately 0.45vol% or more, approximately 0.5vol% or more, approximately 0.6vol% or more, approximately 0.7vol% or more, approximately 0.8vol% or more, approximately 0.9vol% or more or about 1vol% or more.In another example, the sulphur concentration of crude synthesis gas stream 151 can be for about 0.1vol% to about 0.4vol%.Sulphur can exist according to hydrogen sulfide, carbonylsulfide and other form that comprises the compound of sulphur.

Crude synthesis gas in pipeline 151 also can comprise approximately 60vol% or more carbon monoxide and hydrogen, and other component mainly comprises carbonic acid gas and methane.For example the crude synthesis gas in pipeline 151 can comprise approximately 90vol% or more carbon monoxide and hydrogen, approximately 95vol% or more carbon monoxide and hydrogen, approximately 97vol% or more carbon monoxide and hydrogen or approximately 99vol% or more carbon monoxide and hydrogen.In an example, the content of the carbon monoxide of the crude synthesis gas in pipeline 151 can be lower bound approximately 10vol%, approximately 20vol% or about approximately 50vol%, approximately 70vol% or about 85vol% of the paramount limit of 30vol%.In another example, the content of the carbon monoxide of the crude synthesis gas in pipeline 151 can be lower bound approximately 15vol%, approximately 25vol% or about approximately 65vol%, approximately 75vol% or about 85vol% of the paramount limit of 35vol%.The content of the hydrogen of the crude synthesis gas in pipeline 151 can be lower bound approximately 1vol%, approximately 5vol% or about approximately 30vol%, approximately 40vol% or about 50vol% of the paramount limit of 10vol%.For example, the content of the hydrogen of the crude synthesis gas in pipeline 151 can be for about 20vol% to about 30vol%.

Crude synthesis gas in pipeline 151 can comprise less than about 25vol% or less, approximately 20vol% or less, approximately 15vol% or less, approximately 10vol% or nitrogen, methane, carbonic acid gas, water, hydrogen sulfide and hydrogenchloride less or approximately 5vol% or less combination.The content of the carbonic acid gas of the crude synthesis gas in pipeline 151 can be about 25vol% or less, approximately 20vol% or less, approximately 15vol% or less, approximately 10vol% or less, approximately 5vol% or less, approximately 3vol% or less, approximately 2vol% or less or about 1vol% or less.The content of the methane of the crude synthesis gas in pipeline 151 can be about 15vol% or less, approximately 10vol% or less, approximately 5vol% or less, approximately 3vol% or less, approximately 2vol% or less or about 1vol% or less.The content of the water of the crude synthesis gas in pipeline 151 can be about 40vol% or less, approximately 30vol% or less, approximately 25vol% or less, approximately 20vol% or less, approximately 15vol% or less, approximately 10vol% or less, approximately 5vol% or less, approximately 3vol% or less, approximately 2vol% or less or about 1vol% or less.Crude synthesis gas in pipeline 151 can nonnitrogenous gas or is substantially free of nitrogen, for example comprises approximately 0.5vol% or less nitrogen.

Crude synthesis gas in pipeline 151 carries out calorific value that thermosteresis and dilution effect proofread and correct can be approximately 1,863kJ/m ³(50Btu/scf) to approximately 2,794kJ/m ³(75Btu/scf), approximately 1,863kJ/m ³To approximately 3,726kJ/m ³(100Btu/scf), approximately 1,863kJ/m ³To approximately 4,098kJ/m ³(110Btu/scf), approximately 1,863kJ/m ³To approximately 5,516kJ/m ³(140Btu/scf), approximately 1,863kJ/m ³To approximately 6,707kJ/ ³(180Btu/scf), approximately 1,863kJ/m ³To approximately 7,452kJ/m ³(200Btu/scf), approximately 1,863kJ/m ³To approximately 9,315kJ/m ³(250Btu/scf), approximately 1,863kJ/m ³To approximately 10,246kJ/m ³(275Btu/scf), 1,863kJ/m ³To approximately 11,178kJ/m ³(300Btu/scf) or approximately 1,863kJ/m ³To approximately 14,904kJ/m ³(400Btu/scf).

Can control with one or more analyzers 160 speed and the amount of the sulphur that enters into gasifier 150.Described analyzer 160 can for detection of or the amount of measuring sulphur in crude synthesis gas and/or sulphur compound be sulphur content or concentration, and can be with feeder 120 and/or the first locking hopper 110 by 161 communications of communication pipeline, add the gasifier feed in the second locking hopper 130, gasifier feed system 140, pipeline 141 to and/or be directly injected into gasifier 150(with control do not show) gasifier feed in speed and/or the amount of sulphur.Communication pipeline 161 can be wired, wireless or its combination.In another example, described analyzer 160 can send to the staff alarm of sulphur concentration in crude synthesis gas in pipeline 151, and add the gasifier feed in the second locking hopper 130, gasifier feed system 140, pipeline 141 to and/or be directly injected into gasifier 150(do not show) gasifier feed in speed and/or the amount of sulphur can manual regulation or control.

Described analyzer 160 can be placed in the downstream of gasifier 150, for example cross one or more water cooler (not shown)s and/or one or more particulate and remove the element (not shown) to allow in detecting or measuring synthetic gas before sulphur concentration, respectively cooling syngas and/or remove entrained solids (entrained solids).For example, in case synthetic gas be cooled to approximately 600 ℃ or lower, approximately 500 ℃ or lower, approximately 450 ℃ or lower, approximately 400 ℃ or lower, approximately 350 ℃ or lower, approximately 300 ℃ or lower, approximately 250 ℃ or lower, approximately when 200 ℃ or lower temperature, described analyzer 160 can be measured the sulphur concentration of synthetic gas.In another example, in case synthetic gas is cooled to the temperature of 350 ℃, analyzer 160 can be measured the sulphur concentration of synthetic gas.In another example, in case in synthetic gas, the level of particulate is reduced to approximately 10ppmw or lower, approximately 5ppmw or lower, approximately 1ppmw or lower, approximately 0.3ppmw or lower, approximately 0.2ppmw or lower or about 0.1ppmw or lower, analyzer 160 can be measured the sulphur concentration of synthetic gas.

Analyzer 160 can be to estimate, detect or to measure sulphur or the amount of sulphur compound or any analyzer or the technology of concentration in synthetic gas.For example, analyzer 160 can detect, measure or estimate that in addition the crude synthesis gas that leaves flows the sulphur concentration in 151 from gasifier 150 with vapor-phase chromatography, vapor-phase chromatography, gas-liquid partition chromatography.Analyzer 160 can use the narrow pipe of circulation type or post, in gas stream or carrier gas, the different chemical composition of sample is according to their number of chemical and the interaction of physical property and they and specificity column filling, by narrow pipe or the post of described circulation type, described specificity column filling is referred to as static phases with different speed.The passing through of carrier gas can be referred to as mobile (moving) or (mobile) phase that flows.Moving phase can be utilized carrier gas, and described carrier gas includes but not limited to rare gas element such as helium or non-reacted gas such as nitrogen.Analyzer 160 can be also or comprise the arbitrary combination of spectrometer, laser spectrometer, atmospherium, gas separator or aforementioned Analytical equipment or technology.

the detector that can use in analyzer 160 includes but not limited to: flame ionization detector (FID), thermal conductivity detector (TCD), chromatography with discharge ionization detector (DID), electron capture detector (ECD), flame photometric detector (FPD), flame ionization detector (FID), Hall electrolytic conductivity detector (HECD), helium ionization detector (HID), nitrogen phosphorous detector (NPD), infrared detector (IRD), mass selective detector (MSD), photoionization detector(PID) (PID), ionization detector (PDD) is amplified in pulse, heat energy (leading) analyzer/detector (TEA/TCD), mass spectrograph, infrared spectrophotometer, nucleus magnetic resonance (NMR) spectrometer or their combination.

In operation, can come automatically and/or manual regulation feeder 120 according to the signal that transmits in communication pipeline 161 and/or data.Feeder 120 can be percentage feeder or rotary propelling divider (rotofeed dispenser), and can be driven to regulate by variable velocity electric motor (not shown) feeding rate and the amount of sulphur.Sulphur and/or sulphur compound in shortage when analyzer 160 detects crude synthesis gas in pipeline 151 in, be sulphur concentration when first or D score threshold value of predetermined value or expectation are following, can regulate feeder 120 and improve through the sulphur content dispensing of pipeline 122 or be transported to the speed of the gasifier feed in the second locking hopper 130, gasifier feed system 140 and/or pipeline 141.In pipeline 151 in crude synthesis gas sulphur in shortage refer to cumulative volume based on crude synthesis gas in pipeline 151, sulphur concentration is less than about 0.1vol%.

When analyzer 160 detects in pipeline 151 sulphur excessive in crude synthesis gas and/or sulphur compound, be sulphur concentration or concentration expectation second or " on " when threshold value is above, can be automatically and/or manual regulation feeder 120 reduce with pass through the sulphur content dispensing of pipeline 122 or be transported to gasifier feed system 140 speed, the sulphur that passes through pipeline 123 is added to the speed of gasifier feed system 140 and/or will be incorporated into speed in gasifier 150 by pipeline 141 through the sulphur of pipeline 124.For example,, when the sulphur concentration in crude synthesis gas in pipeline 151 is increased to higher than about 0.4vol%, approximately 0.5vol%, approximately 0.6vol%, approximately 0.7vol%, approximately 0.8vol%, about 0.9vol% or approximately during 1vol%, can reduce and/or stop being incorporated into the amount of the sulphur of gasifier feed in the second locking hopper 130, gasifier feed system 140 and/or pipeline 141.With this mode can automatic or manual control sulphur concentration in crude synthesis gas stream 151 with sulphur concentration within keeping predetermined or expected range, to reduce or to stop metal dusting in gasifier 150 downstream components.

Consider in more detail gasifier 150, gasifier 150 can be or comprise one or more solid circles or transport gasifier, one or more fixed bed gasifiers, one or more fluidized-bed gasifier, one or more entrained flow gasifiers or their combination.For example, the solid circle gasifier can operate in the following manner: one or more oxygenants are incorporated in incoming flow, for example through the gasifier feed of pipeline 141, and/or be incorporated in the (not shown) of one or more mixing zones so that gaseous mixture to be provided.In another example, oxygenant directly can be added in gasifier.Be incorporated into the type of the oxygenant in the solid circle gasifier and measure composition and the physical property that can affect through the synthetic gas of pipeline 151, and therefore affecting the downstream product by their preparations.Described one or more oxygenants can be incorporated in one or more mixing zones to generate gaseous mixture, and for example can introduce according to the speed of the temperature that is suitable for controlling mixing zone.Gaseous mixture can be moved upwards up in riser tube (riser) (not shown) by mixing zone, in the riser tube residence time, can allow char gasification, methane/steam formation, tar cracking and/or water-gas shift occurs.The temperature of mixing zone can be for starting from approximately 500 ℃ to approximately 650 ℃ and be increased to approximately 900 ℃, if for example crushed coke or Equivalent are fed in this mixing zone.In an example, riser tube can operate at the temperature higher than mixing zone.Gaseous mixture can leave riser tube and enter one or more settling vessels (disengager) or cyclonic separator (cyclone) (not shown), here large particulate can separate from gas and recycle back to mixing zone.

The residence time in the solid circle gasifier can be approximately 2 seconds or more grow to approximately 10 seconds or longer, and wherein water-gas shift is reached balance can be enough (being the approximately about temperature of 1,000 ℃ of 250 ℃ of paramount limits of lower bound) to temperature.The service temperature of solid circle gasifier can be controlled in the following manner at least in part: the recirculation rate by solid in riser tube and the residence time, by falling low-ash temperature before being recycled to mixing zone, by steam being added to mixing zone and/or by adding oxygenant to mixing zone.The solid of recirculation can be used for the gasifier feed that rapid heating enters through pipeline 141, and it can make the tar formation minimum that is reduced to.Mixing zone can operate at approximately 100 kPas (kPa) to the pressure of about 4500kPa, with the heat output that increases per unit reactor cross-section area and improve energy output in any power cycle subsequently.

Because the temperature out of solid circle gasifier can be pro rata less than comparable gasifier (for example slag type), in synthetic gas, the amount of the amount of heat and chemical heat can be less comparably in the solid circle gasifier., due to the service temperature that reduces in gasifier (namely less than 1,600 ℃), can consume less energy and control and optimize H ₂: the CO ratio, thus can steam demand not have with increasing the output of hydrogen under the prerequisite of amount increase in gasifier.The solid circle gasifier that is fit to can be as the 7th, 722, discusses and describe in No. 690 United States Patent (USP)s and the 02008/0155899th, 2009/0151250 and No. 2009/0188165 U.S. Patent application.

In another example, operate in the top that fixed bed or moving-bed gasification device can be by will be incorporated into through the gasifier feed of pipeline 141 reactor or top (not shown) part.Oxygen and/or steam can be incorporated into the bottom that is positioned at reactor or the fixed bed gasifiers of bottom.Charging can move down by reactor and can be vaporized by gravity.In gasification, remaining ash content can withdraw from the bottom of reactor.Fixed bed gasifiers can and be compared the oxygen that can need less amount in the lower operation of relatively low temperature out (425 ℃ to 700 ℃) with entrained flow gasifiers with fluidized-bed gasifier, but steam is had high request and produces a large amount of tar.Fixed bed gasifiers can have the ability of limited processing fine powder and for processing caking coal, have special demands.Product synthetic gas from fixed bed gasifiers can comprise unconverted methane and/or by product tar and oil.The fixed bed gasifiers that is fit to can be as the 4th, 290,780,4,417,528 and 5,069, and in No. 685 United States Patent (USP)s and No. 2008/0086945 U.S. Patent application, institute discusses and describes.

In another example, can mix to come operating fluidized bed gasifier in the reactor (not shown) by the particle that will grow (older) from the gasifier feed through pipeline 141 and time, partly gasify and/or all gasify.Can use gas fluidized solids, then can divided gas flow and remaining solids.Gas in reactor can comprise oxygen, steam, recirculation synthetic gas or their combination.Gas can be to be enough to floating solids to the stream in reactor, and not with solids sucking-off reactor.Fluidized-bed gasifier can operate under medium temperature out, and temperature can be consistent in whole bed.For example, fluidized-bed gasifier can be in approximately 700 ℃ of lower bounds, approximately 750 ℃, approximately 800 ℃, approximately approximately 1,000 ℃, approximately 1,050 ℃ of 850 ℃ of paramount limit, approximately 1,100 ℃ or approximately operate at the temperature of 1,150 ℃.Fluidized-bed gasifier can need than the more substantial oxygen of comparable fixed bed gasifiers but need the oxygen of less amount than comparable entrained flow gasifiers.Similarly, fluidized-bed gasifier can need than comparable fixed bed gasifiers still less steam but than the more steam of comparable entrained flow gasifiers needs.Synthetic gas from fluidized-bed gasifier can recently have higher purity from comparable entrained flow gasifiers, and the conversion of carbon can be lower than comparable entrained flow gasifiers.Purity can be by the H in synthetic gas ₂The amount of+CO is measured.For example, in fluidized-bed gasifier, the purity of synthetic gas can be for 25% to 90%H ₂+ CO.Carbon in fluidized-bed gasifier transforms and can be about 92%, the approximately 93% or approximately 94% paramount limit approximately 97%, approximately 98% or approximately 99% of lower bound for example.Suitable fluidized-bed gasifier can be as the 4th, 696,678,6,972,114 and 7,503, and discuss and describe in No. 945 United States Patent (USP)s and No. 2008/0250714 U.S. Patent application.

In another example, entrained flow gasifiers can be injected in reactor beds and operate by the gasifier feed through pipeline 141 with in parallel-flow and oxygenant.Gasifier feed heats up rapidly and and oxidant reaction.Described oxygenant can be oxygen, steam, recirculation synthetic gas or their combination.Entrained flow gasifiers can need a large amount of oxygenants and can need high oxygen purity.For example, entrained flow gasifiers can need approximately 0.2 standard cubic meter (" Nm ³") O ₂To about 0.5Nm ") O ₂Every Nm ³(H ₂+ CO).In addition, the oxygenant that is incorporated into entrained flow gasifiers can have approximately 99.5% or higher purity.Entrained flow gasifiers can operate and usually need high-temperature to realize high efficiency of carbon conversion under high-temperature.For example, entrained flow gasifiers can be in approximately 1,150 ℃ of lower bound, approximately 1,200 ℃, approximately 1,250 ℃ or approximately approximately 1,550 ℃, approximately 1,600 ℃ of 1,300 ℃ of paramount limit, approximately 1,650 ℃ or approximately operate at the temperature of 1,700 ℃.Entrained flow gasifiers also can need the energy input higher than fixed bed gasifiers, and described energy input is higher steam rate and/or the form of oxygen consumption gas rate.Material in entrained flow gasifiers can obtain highly purified synthetic gas and can gasify very on a large scale.For example, can have less than about 0.5% N from the synthetic gas of entrained flow gasifiers ₂, without the methane of tar and ppm.Entrained flow gasifiers can have the short residence time, i.e. lower bound approximately 0.1 second, approximately 0.2 second or about 0.3 second paramount limit approximately 1 second, approximately 2 seconds or approximately 3 seconds.Suitable entrained flow gasifiers can be as the 4th, 158,552,4,531,949 and 5,620, and in No. 487 United States Patent (USP)s and No. 2010/0088959 U.S. Patent application, institute discusses and describes.

Fig. 2 has described according to one or more embodiments, for the production of the schematic diagram of another illustrative gasification system 200 through the synthetic gas of pipeline 251, the sulphur concentration that described synthetic gas has is enough to be reduced in the metal dusting in the downstream components of one or more gasifiers (one is shown as 250)., with above similar with reference to embodiment that Fig. 1 discussed and described, sulphur can be stored in one or more the first locking hoppers or storage hopper 110.The first locking hopper 110 can with first or " sulphur " feeder 220 directly or through pipeline 111 be communicated with.The first feeder 220 can be distributed to one or more the second locking hoppers 130 through

pipeline

221 and 222 with the sulphur from the first locking hopper 110.The first feeder 220 can be controlled amount and/or the speed of distributing to the sulphur of the second locking hopper 130 through pipeline 221.For example, the first feeder 220 can be percentage feeder or rotary propelling divider, and can be driven by variable velocity electric motor (not shown).Before being fed to the first locking hopper 110 and/or the first feeder 220, sulphur can be polished (pulverized) or grind (ground) become powder and after grinding average granularity can be above with reference to the first locking hopper 110 in Fig. 1 with feeder 120 is discussed and the size of description.

The second locking hopper 130 can receive, stores and/or mix through the raw material of pipeline 101 and the sulphur of process pipeline 222, and can transport or be dispensed to gasifier feed system 240 through the carbonaceous material that comprises sulphur of pipeline 239.Alternatively, can directly add sulphur to gasifier feed system 240, walk around the second locking hopper 130.For example, the sulphur through pipeline 223 can be added in one or more storage hoppers 242 of gasifier feed system 240, replace adding the sulphur through

pipeline

221 and 222 to second locking hopper 130.

The second locking hopper 130 can be with the second feeder 234 in conjunction with through pipeline 231, operating, described the second feeder is as the high-voltage rotary feeder of the fluid steam (not shown) cooperation with adding, so that carbonaceous material is transported to gasifier feed system 240 through pipeline 239.The illustrative fluid can include but not limited to air, nitrogen, carbonic acid gas or their arbitrary combination.Preferably, can be according at least 10, the speed of 000kg/h and more preferably with approximately 20, the paramount limit of 000kg/h approximately 30, the speed of 000kg/h is transported to gasifier feed system 240 with carbonaceous material from the second locking hopper 130.

Gasifier feed system 240 can be accepted through pipeline 239 and/or from the carbonaceous material that comprises sulphur of another technique or source (not shown) and the gasifier feed that pipeline 241 is passed through in generation.Gasifier feed system 240 can comprise storage hopper 242, one or more first or " locking (lock) " container 244, one or more second or " distribution " container 246, and one or more the second feeder 248.Storage hopper 242 can be connected with locking container 244 and/or with locking container 244 fluids, be communicated with by one or more the first control valves 243, and storage hopper 244 can be connected with distribution container 246 and/or with distribution container 244 fluids, be communicated with by one or more the second control valves 245.

Carbonaceous material from the second locking hopper 130 can be incorporated into storage hopper 242 through pipeline 239 and any extra sulphur through pipeline 223.Can add nitrogen to storage hopper 242 to keep the air pressure in storage hopper 242 through low-pressure nitrogen source 202.The sulphur that adds storage hopper 242 to can mix to provide the carbonaceous material that comprises sulphur in locking container 244 and/or distribution container 246 with the carbonaceous material in storage hopper 242.

Carbonaceous material through pipeline 239 can have or not have the sulphur of interpolation and can be dried and/or pulverize.For example, the carbonaceous material through pipeline 101 can be dried and can pulverize by one or more pulverizing mill (not shown)s before being fed to the second locking hopper 130.For example, can be dried to approximately 22% to about 15% moisture through the raw material of pipeline 101.In another example, the raw material through pipeline 101 can be dried to approximately 18% moisture.In one or more embodiments, can carry out dry raw material through pipeline 101 with the fluidized bed dryer (not shown).Carbonaceous material through pipeline 239 can be dried and can pulverize by one or more pulverizing mill (not shown)s before being fed to storage hopper 242.Described pulverizing mill can comprise, for example one or more bowl mills or one or more rod milling (not shown).

Can be with the carbonaceous material that comprises sulphur from storage hopper 242 with controlled speed or be fed to off and in locking container 244.Can locking container 244 be separated from storage hopper 242 by sealing the first control valve 243.Can use through 203 pairs, the first high pressure nitrogen source locking containers 244 and be forced into first or " holonomic system " pressure.

The first pressure in locking container 244 can be lower bound approximately 2,400kPa, approximately 2,600kPa, approximately 2,800kPa or approximately 3, the paramount limit of 000kPa approximately 4,000kPa, approximately 4,200kPa, approximately 4,400kPa or approximately 4,600kPa.For example, the first pressure in locking container 244 can be approximately 2, and 500kPa is to approximately 4, and 500kPa, approximately 2,700kPa be to approximately 4, and 300kPa or approximately 2,900kPa be to approximately 4,100kPa.In another example, the first pressure can be approximately 3,500kPa.Distribution container 246 can remain on the first pressure.

In case the carbonaceous material that comprises sulphur in locking container 244 reaches the first pressure, namely the pressure of distribution container 246, can open the second control valve 245 between locking container 244 and distribution container 246.Then, can be fed in distribution container 246 by the carbonaceous material that gravity will comprise sulphur, until the complete inventory of locking container 244 all is discharged into distribution container 246.Then, locking container 244 can be separated with distribution container 246 and reduce pressure and prepare to receive another time discharging from the carbonaceous material that comprises sulphur of storage hopper 242.

Distribution container 246 can operate continuously under the first pressure.Can keep with the nitrogen through the second high pressure nitrogen source 204 pressure in distribution container 246.The carbonaceous material that comprises sulphur can be transported to one or more gasifiers 250 from the bottom of distribution container 246 by the second feeder 248.

The second feeder 248 can be without the on-mechanical feed control device of moving parts and continuous ash content depressurized system and traditional design combination can be used for flow rate control.The mobile motivating force of the carbonaceous material that comprises sulphur that is used for feeder 248 can be pressure reduction wherein.Press the nitrogen gas in nitrogen source 205 and through the transporting fluid in transporting fluid source 206 through third high, for example the synthetic gas of air and/or recirculation can be to by feeder 248 and leave feeder 248 and measure to the flow of the carbonaceous material that comprises sulphur of gasifier 250.

The gasifier feed of advancing pipeline 241 can be incorporated into gasifier 250 to generate crude synthesis gas stream 251.Gasifier feed in pipeline 241 can be dry charging or as slurry or suspension, be transported to gasifier.Gasifier 250 can be but be not limited to, one or more solid circle gasifiers, one or more fixed bed gasifiers, one or more fluidized-bed gasifier, one or more entrained flow gasifiers or their combination.

Gasifier 250 can comprise single reactor row (reactor train) or two or more reactors row of connecting or being arranged in parallel.Each reactor row can comprise one or more mixing zones 252, one or more riser tube 253 and one or more settling vessel 254.Each reactor row can configure or be configured to share one or more mixing zones 252, riser tube 253 or settling vessel 254 arbitrarily independently of one another.For simplicity and the easiness described, the embodiment of gasifier 250 will further describe in the context of single reactor row.

Can make up to provide gaseous mixture or suspension in mixing zone 252 through the gasifier feed of pipeline 241 and one or more oxygenants or the processing air of process pipeline 214.As shown, can be injected into respectively mixing zone 252 or mixed (not shown) before being injected into mixing zone through the gasifier feed of pipeline 241 and the oxygenant of process pipeline 214.For example, can sequentially be injected into gasifier 250 through the gasifier feed of pipeline 241 and the oxygenant of process pipeline 214.In another example, can be injected into simultaneously in gasifier 250 through the gasifier feed of pipeline 241 and the oxygenant of process pipeline 214.

The type and the amount that are incorporated into the oxygenant of gasifier 250 through pipeline 214 can affect composition and physical property through the synthetic gas of pipeline 251, and therefore affect downstream product prepared therefrom.One or more oxygenants can include but not limited to: air, oxygen, be oxygen (essentially oxygen), oxygen-rich air (oxygen-enriched air), oxygen and mixture, oxygen and the rare gas element of air such as the mixture of nitrogen and argon gas etc. substantially.Oxygenant can comprise approximately oxygen or oxygen more, approximately 70vol% or oxygen more, approximately 75vol% or oxygen more, approximately 80vol% or oxygen more, approximately 85vol% or oxygen more, approximately 90vol% or oxygen more, approximately 95vol% or the oxygen more or approximately 99vol% or more of 65vol%.As used in this article, term " being oxygen substantially " refers to comprise oxygen or the more Oxygen Flow of 51vol%.As used in this article, term " oxygen-rich air " refers to comprise oxygen or the more air of 21vol%.Oxygen-rich air can for example obtain from low-temperature distillation, pressure-variable adsorption, membrane sepn or their arbitrary combination of air.At least a in oxygenant can be the purity oxygen that is provided by one or more air separation equipment (not shown)s.One or more oxygenants can nonnitrogenous gas or are substantially free of nitrogen.So-called " being substantially free of nitrogen ", the meaning be one or more oxygenants comprise the nitrogen of about 5vol% or still less, approximately 4vol% nitrogen or still less, approximately 3vol% nitrogen or still less, approximately nitrogen or the still less or about nitrogen or still less of 1vol% of 2vol%.

Gaseous mixture can be moved upward in riser tube 253 by mixture 252, and in riser tube 253, the extra residence time allows char gasification, methane/steam formation, tar cracking and/or water-gas shift occurs.Riser tube 253 can operate and can have the diameter less than mixing zone 252 at than the higher temperature in mixing zone 252.In riser tube 253, suitable temperature can be approximately 700 ℃ of lower bounds, approximately 715 ℃, approximately 730 ℃ or about approximately 950 ℃, approximately 1,000 ℃, approximately 1,050 ℃ or approximately 1,100 ℃ of 750 ℃ of paramount limit.For example, in riser tube 253, suitable temperature can be approximately 710 ℃ to approximately 1,075 ℃, approximately 720 ℃ to approximately 1,025 ℃ or approximately 740 ℃ to approximately 975 ℃.In riser tube 253, surface gas speed can be lower bound approximately 3 meter per seconds (m/s), approximately 6m/s or about approximately 21m/s, approximately 24m/s or about 27m/s of the paramount limit of 9m/s.For example, in riser tube 253 surface gas speed can for about 5m/s to about 25m/s, approximately 10m/s to about 18m/s or approximately 9m/s to about 12m/s.

Gaseous mixture can leave riser tube 253 and enter settling vessel 254, larger particle can separate and pass through one or more conduit recycle back to mixing zone 252 from gas in settling vessel 254, and described conduit includes but not limited to: vertical tube 259 and/or j shape support (j-leg) 258.J shape support 258 can comprise that non-mechanical " j-valve " increases effective solid retention time, improves carbon and transforms and make solids recirculation 252 inflation requirements minimizes to mixing zone.In one or more embodiments, settling vessel 254 can be cyclonic separator.One or more particulate transporters 257 can be placed in the downstream of settling vessel 254, be used for collecting the fine-particle powder that separates, described particulate transporter 257 is one or more seal valves (loop seals) or seal leg (seal legs) for example.Although do not show.Subordinate phase scale trap or cyclonic separator can be placed or be placed on vertical tube 259, be used for isolating most micro-solid from the top of settling vessel 254.Any carry secretly or remaining particulate all can use one or more particulate removal systems or particulate control device 290 to remove in crude synthesis gas stream 251.Can be with through pipeline 208, for example the recycle gas from the compressor (not shown) joins j shape support 258, particulate transporter 257, vertical tube 259 or their arbitrary combination, be used for inflation to help solid circulation.

Can introduce through one or more oxygenants of pipeline 214 bottom of mixing zone 252, with the temperature of raising mixing zone 252 and riser tube 253 and any carbon in the recirculation particulate that is included in ash content (" coal tar (char) ") form that burns.For example, can one or more oxygenants be incorporated into mixing zone 252 according to the speed that is suitable for controlling mixing zone 252 temperature.Described one or more oxygenants can comprise excessive air.For example, described one or more oxygenants can be the air of stoichiometry deficiency, and wherein the mol ratio of oxygen and carbon can be maintained at the concentration of stoichiometry deficiency, thereby help the formation of the 252 interior carbon monoxide in mixing zone to surpass carbonic acid gas.In another example, being provided to the oxygen of mixing zone 252 by oxygenant can be less than 5% of the chemical dose of the needed oxygen of burning of completing all carbon that offer mixture 252.Oxygen and steam extra in air can be by the coal tar consumption in recirculated solids, to stablize temperature of reactor during operation and at the charging intercourse.

The interior residence time of gasifier 250 and temperature can be enough to make water-gas shift reach balance.For example, through residence time of the gasifier feed of pipeline 241 in mixing zone 252 can greater than approximately 2 seconds, greater than approximately 5 seconds or greater than approximately 10 seconds.The service temperature of gasifier 250 can be approximately 600 ℃ of lower bounds, approximately 650 ℃ or about approximately 900 ℃, approximately 1,000 ℃ or approximately 1,100 ℃ of 700 ℃ of paramount limit.For example, the service temperature of gasifier 250 can be approximately 625 ℃ to approximately 1,050 ℃, approximately 675 ℃ to approximately 1,025 ℃ or approximately 700 ℃ to approximately 975 ℃.

Gasifier 250 can operate within being enough to not melt the temperature range of ash content, for example approximately 565 ℃ to approximately 1040 ℃ or approximately 840 ℃ to approximately 930 ℃.Heat can by recirculated solids with enter before gasifier feed through pipeline 241 contacts, the carbon in the solid circle of burning 252 bottoms, mixing zone provides.Can reach approximately 500 ℃ to the about temperature and randomly of 650 ℃ by making mixing zone 252, by coke breeze or other solids, liquid or gaseous fluid are fed to mixing zone 252 with the temperature that further increases mixing zone 252 to approximately 900 ℃ start to start.

Starting burner 215 can be used for starting gasifier 250 through pipeline 216.The fuel that starts burner 215 can be supplied with by the starting fluid pipeline through pipeline 233.The oxygenant or the process air that are used for startup burner 215 can be supplied with by pipeline 214.Start burner 215 and can be the burner of propane of directly burning, the operation of combustors of described burning propane is used for heating gasifying device 250 to approximately 500 ℃ to approximately 650 ℃.Liquid fuel, for example fuel oil, also can use based on their operability.Starting burner 215 can be at about 500kPa to starting under the system pressure of about 550kPa and can, at about 950kPa to approximately 1, operating under the pressure of 050kPa.

Temperature variation in gasifier 250 can be subject to a large amount of solid of circulation in gasifier 250 and suppress.Described solid circle also can be used for the gasifier feed through pipeline 241 that rapid heating is introduced, and this can make tar formation minimizing.

Mixing zone 252 can about 100kPa to operation under the pressure of about 4500kPa with the heat output that improves the reactor cross-section unit surface and the energy output in improving any power cycle subsequently.For example, mixing zone 252 can be at about 250kPa to approximately 4000kPa, 500kPa to about 3000kPa or approximately 750kPa operate to the pressure of about 2500kPa.

Crude synthesis gas in the pipeline 251 that produces in gasifier 250 can be with above similar with reference to the crude synthesis gas in the pipeline 151 that Fig. 1 discussed and described.Steam can be with the mixing zone that is added into gasifier together with the oxidant stream of pipeline 214 so that the point of introducing at oxygenant makes the temperature rising slow down.Also steam can be offered the mixing zone of gasifier 250 with the ratio (H of the hydrogen in control gasifier 250 with carbon monoxide ₂: CO).Because the temperature out of gasifier 250 can be pro rata less than comparable gasifier (as the slag type), through the amount of the amount of the heat in the crude synthesis gas of pipeline 251 and chemical heat gasifier 250 is interior can be comparably less.Steam can be used for consuming to regulate change H by using than other entrained flow gasifiers that operates energy still less under higher temperature ₂: the CO ratio., due to the service temperature (that is, less than 1,600 ℃) of gasifier 250 interior reductions, can consume still less energy and control and optimize H ₂: the CO ratio, thus in the situation that there is no to increase with amount the output of increase hydrogen aspect the steam demand in gasifier 250.Leave gasifier 250, the H of the crude synthesis gas of process pipeline 251 ₂: CO can be for about 0.6:1 to about 1.3:1.For example, H ₂: the ratio of CO can for about 0.7:1 to about 1.2:1, approximately 0.8:1 to about 1.1:1 or approximately 0.9:1 to about 1:1.

Gasifier bottom blow-down tank 255 can be used for making the ash content from gasifier 250 go stockization (de-inventory) during preventive repairing.In vertical tube 259, the ash content of other accumulation can from particulate transfer devices, for example be removed the ash content level that keeps vertical tube 259 interior from seal leg.Can store and/or processed through pipeline 256 chargings from the solid of gasifier bottom blow-down tank 255.

Crude synthesis gas in pipeline 251 can approximately 575 ℃ to approximately leaving gasifier at the temperature of 1,050 ℃.Before entering particulate removal systems 290, can use one or more water cooler 270(" primary cooler ") crude synthesis gas in cooling pipeline 251 to be to provide cooling crude synthesis gas stream 286.

Water cooler 270 can comprise that the heat exchanger of one or more arranged in series or heat exchange zone (have shown three: 271,280 and 285).Crude synthesis gas in pipeline 251 can be in the first heat exchanger (" the firstth district ") 271 be cooled to approximately 260 ℃ to the about temperature of 820 ℃ by heat exchange indirectly.The cooling crude synthesis gas that leaves the first heat exchanger 271 by pipeline 272 can further be cooled to approximately 260 ℃ to the about temperature of 705 ℃ by heat exchange indirectly in the second heat exchanger (" Second Region ") 280.The cooling crude synthesis gas that leaves the second heat exchanger 271 by pipeline 282 can further be cooled to approximately 260 ℃ to the about temperature of 430 ℃ by heat exchange indirectly in the 3rd heat exchanger (" the 3rd district ") 285.

Can carry out crude synthesis gas in cooling pipeline 251 with heat-transfer medium.Described heat-transfer medium can be saturated steam, oiler feed etc.Heat-transfer medium through pipeline 283 can be incorporated in syngas cooler 270.Heat from crude synthesis gas can be transferred to indirectly heat-transfer medium can be through the overheated or high pressure superheated steam of pipeline 281 recovery to provide.Overheated or high pressure superheated steam through pipeline 281 can be used to one or more steam turbine (not shown)s that power is provided, and described steam turbine for example can drive direct-coupled generator (not shown).The phlegma that reclaims from steam turbine can be used as oiler feed recirculation with cooling syngas and generating steam.

Heat-transfer medium through pipeline 283 can heat to provide the oiler feed through cooling synthetic gas and the process pipeline 287 of pipeline 286 in the 3rd heat exchanger (" economizer ") 285.Under processing conditions, can make saturated or basically saturated through the oiler feed of pipeline 287.Can will be incorporated into through the oiler feed of pipeline 287 in (" flash evaporation is to (flash) ") one or more steamdrums or separator 275, to provide water through the heating of pipeline 277 to be fed in vapour generator 271.

From the temperature through the overheated or high pressure superheated steam of pipeline 281 of syngas cooler 270 can for approximately 400 ℃ or higher, 425 ℃ or higher, 450 ℃ or higher, 475 ℃ or higher, 500 ℃ or higher or 550 ℃ or higher.The pressure of the overheated or high pressure superheated steam of process pipeline 281 can be 4,000kPa or higher, approximately 4,500kPa or higher, approximately 5,000kPa or higher, approximately 5,550kPa or higher, approximately 6,000kPa or higher, approximately 6,500kPa or higher, approximately 7,000kPa or higher or approximately 7,500kPa or higher.

The oiler feed through pipeline 277 of self-separation device 275 in the future is incorporated in the first heat exchanger (" vapour generator ") 271, and to the heating of the crude synthesis gas in pipeline 251, thereby generate the steam that be directed into separator 275 by pipeline 273.The steam that turns back to separator 275 through pipeline 273 can leave by pipeline 276, provide steam through the overheated or high pressure superheater of pipeline 281 thereby be used for carrying out superheat at the second heat exchanger 280, this steam overheated or high pressure superheater uses in one or more steam turbine (not shown)s.Can be controlled at by a small amount of water through pipeline 278 of discharging (blow down) accumulation of solid in separator 275.

Heat exchanger 271,280,285(have shown three) in any one or can be all shell and-tube heat exchanger.Crude synthesis gas in pipeline 251 can supply to shell-side or the pipe side of the first heat exchanger 271, the second heat exchanger 280 and the 3rd heat exchanger 285 continuously.According to crude synthesis gas being incorporated into which journey, heat-transfer medium can be by shell-side or pipe side.In one or more embodiments, crude synthesis gas in pipeline 251 can be supplied to abreast shell-side or the pipe side and according to crude synthesis gas being incorporated into which side of the first heat exchanger 271, the second heat exchanger 280 and the 3rd heat exchanger 285, heat-transfer medium can be continuously by shell-side or pipe side.Can add supplementary (make-up) heat-transfer medium by pipeline 283.

Cooling synthetic gas through pipeline 286 can be incorporated into particulate removal systems 290, with partially or even wholly remove the particulate that carrys out self cooled synthetic gas with provide through the separation of pipeline 291, " (particulate-lean) of humble grain " or " clean (clean) " synthetic gas, through the particulate of the separation of pipeline 292 with through the condensation product of pipeline 293.Between the starting period, the steam through pipeline 288 can be offered particulate removal systems 290 so that it is carried out preheating.Although show, described one or more particulate removal systems 290 can randomly be used for the cooling particulate of partially or completely removing before from the crude synthesis gas of pipeline 251.For example, the crude synthesis gas in pipeline 251 can be introduced directly into particulate removal systems 290, cause the gas particles of heat to remove (for example, approximately 550 ℃ to approximately 1,050 ℃).Although do not show, can use two particulate removal systems 290.For example, particulate removal systems 290 can be in the downstream of water cooler 270 in upstream and a particulate removal systems 290 of water cooler 270.

One or more particulate removal systems 290 can comprise one or more tripping devices, for example conventional separator and/or cyclonic separator (not shown).Can provide the particulate control device (" PCD ") of outlet particulate loading below the detectability of about 0.1ppmw but also can use.The PCD of illustrative can include but not limited to: but sintering metal filter, metal filtration post (metal filter candles) and/or ceramic filter post (ceramic filter candle) (for example, iron aluminide filter material).Can carry out the pulse cleaning strainer with a small amount of high pressure recirculation synthetic gas through pipeline 289, because they can accumulate the particulate from unfiltered synthetic gas.

One or more analyzers (having shown two 260,265) can be placed in the downstream of gasifier 250 to detect amount or the sulphur concentration from gasifier 250 sulphur out.Analyzer 260,265 can connect the 261,266 and/or 267 and first feeder 220 and/or the first locking hopper 110 communications by communication, so that the sulphur concentration in control and/or maintenance gasifier 250 and/or crude synthesis gas stream 251.Communication device 261,266 and/or 267 can be wired, wireless or their combination.

Thereby temperature is the cold tempering system (not shown) that is sent to enough, and the sulphur concentration that is positioned at the point of the treatment system upstream that can change arbitrarily the synthetic gas sulphur concentration can be measured by the analyzer 260,265 in gasifier 250 downstreams, and described treatment system for example is the alkali cleaning step.For example, after it was cooled by water cooler 270, the first analyzer 260 can be measured the sulphur concentration in the cooling synthetic gas of this process pipeline 286 through the synthetic gas of pipeline 286.In another example, after it had passed through particulate removal systems 290, the second analyzer 265 can be measured the sulphur concentration in the synthetic gas of separation of this process pipeline 291 through the synthetic gas of pipeline 291.In another example, the first analyzer 260 can be measured through the sulphur concentration in the cooling synthetic gas of pipeline 286 and the second analyzer 265 and can measure through the sulphur concentration in the synthetic gas of the separation of pipeline 291.Analyzer 260,265 can be but be not limited to: gas chromatograph, atmospherium, gas separator or their arbitrary combination.Analyzer 260,265 can be with above identical or similar with reference to analyzer 160 that Fig. 1 discussed and described.

In case analyzer 260,265 is measured or measured through the sulphur concentration in the synthetic gas of the separation of the cooling synthetic gas of pipeline 286 and/or process pipeline 291, analyzer 260,265 can output to operator's (not shown), the first feeder 220 and/or the first locking hopper 110 with signal and/or data by communication device 261,266 and/or 267.For example, the first analyzer 260 can pass through communication device 261 and the 267 and first feeder 220 and/or the first locking hopper 110 communications.In another example, the second analyzer 265 can pass through communication device 266 and the 267 and first feeder 220 and/or the first locking hopper 110 communications.In another example again, analyzer 260,265 both can pass through communication device 261,266 and/or 267 and the feeder exchange of information.Although show, the communication of the first feeder 220 and/or the first locking hopper 110 and order about (actuation) and can promote by operator and/or control unit, described operator and/or control unit can be in this locality of system 200 or are long-range.

In operation, can regulate the first feeder 220 according to signal and/or data that communication device 267 transmits.When the first analyzer 260 and/or the second analyzer 265 detect sulphur in shortage in the cooling synthetic gas through pipeline 286 and/or the synthetic gas through the separation of pipeline 291, while being sulphur concentration lower than the concentration of expectation, can regulate the first feeder 220 increases that will join or be transported to the speed of gasifier feed system 240 and/or increase through the sulphur content of pipeline 222 will be through the speed of the storage hopper 242 of the sulphur content dispensing gasifier feed system 240 of pipeline 223.Can be defined as through sulphur in shortage in the cooling synthetic gas of pipeline 286: based on the cumulative volume of the cooling synthetic gas in pipeline 286, sulphur concentration is lower than about 0.05vol%, approximately 0.1vol% or about 0.2vol%.Can be defined as through sulphur in shortage in the synthetic gas of the separation of pipeline 291: based on the cumulative volume of the synthetic gas of the separation in pipeline 291, sulphur concentration is lower than about 0.05vol%, approximately 0.1vol% or about 0.2vol%.

In analyzer 260,265 detects through the cooling synthetic gas of pipeline 286 and/or the synthetic gas through the separation of pipeline 291 during excessive sulphur, be sulphur concentration when too high, can regulate the first feeder 220 and reduce that will join or be transported to the speed of locking hopper 130 and/or reduce through the sulphur content of pipeline 222 will be through the speed of the storage hopper 242 of the sulphur content dispensing gasifier feed system 240 of pipeline 223.For example,, when be increased to approximately 0.3vol%, approximately 0.4vol% or approximately 0.5vol%, approximately 0.6vol%, approximately 0.7vol%, approximately 0.8vol%, about 0.9vol% or when approximately 1vol% is above through sulphur concentration in the cooling synthetic gas of pipeline 286, can reduce or stop being assigned to the amount of the sulphur of locking hopper 130 and/or gasifier feed system 240.In another example,, when sulphur concentration in the synthetic gas through the separation of pipeline 291 is increased to approximately 0.3vol%, approximately 0.4vol% or approximately 0.5vol%, approximately 0.6vol%, approximately 0.7vol%, approximately 0.8vol%, about 0.9vol% or when approximately 1vol% is above, can reduce or stop being assigned to the amount of the sulphur of locking hopper 130 and/or gasifier feed system 240.

, based on the sulphur concentration that detects by analyzer 260,265 (or multiple concentration), to all adjustings of the first feeder 220, can be automatic adjusting.In another example, adjusting can be ordered about by the controller (not shown), described controller by communication device 261,266,267 or other communication device (not shown)s receive from analyzer 260,265 one or more signals and/or data.The signal and/or the data that send based on analyzer 260,265, the amount of the sulphur that also can manual regulation distributes by the first feeder 220.

Embodiment of the present disclosure further relate in following paragraph any one or more snippets:

1. method that be used for to keep the synthetic gas sulphur concentration, described method comprises: sulphur and carbonaceous material are made up to generate the carbonaceous feed that comprises sulphur; Make at least a portion gasification of sulphur concentration in synthetic gas; And, based on the sulphur concentration that detects, regulate the amount of adding the sulphur in carbonaceous material to.

2. the 1st section described method, wherein said carbonaceous material comprises coal, coke, oil, biomass or their arbitrary combination.

3. the 1st section or the 2nd section described method, wherein said synthetic gas has the sulphur concentration of expectation, and described sulphur concentration is 0.1vol% at least.

4. according to any one section described method in the 1st to 3 section, the mean particle size of wherein said carbonaceous material is approximately 50 microns to approximately 500 microns.

5. the 4th section described method, the mean particle size of the sulphur of wherein said interpolation is approximately 50 microns to approximately 500 microns.

6., according to any one section described method in the 1st to 5 section, wherein with vapor-phase chromatography, spectrometry, vapor-phase chromatography, gas-liquid partition chromatography or their combination, detect sulphur.

7. the 6th section described method, the wherein said mean particle size that comprises the carbonaceous mixture of sulphur is approximately 400 microns or less.

8. according to any one section described method in the 1st to 7 section, the wherein said carbonaceous feed that comprises sulphur gasifies in the transportation gasifier.

9. according to any one section described method in the 1st to 7 section, the wherein said carbonaceous feed that comprises sulphur gasifies in fluidized-bed gasifier.

10. according to any one section described method in the 1st to 7 section, the wherein said carbonaceous feed that comprises sulphur gasifies in entrained flow gasifiers.

11. according to any one section described method in the 1st to 7 section, the wherein said carbonaceous feed that comprises sulphur gasifies in fixed bed gasifiers.

12. a method that is used for keeping the synthetic gas sulphur concentration, described method comprises: sulphur is added to the carbonaceous feed that comprises sulphur in carbonaceous material with generation, described carbonaceous feed comprises the sulphur of 0.05vol% at least; The carbonaceous feed that will comprise sulphur is incorporated in the transportation gasifier to generate synthetic gas; Detect the sulphur concentration in synthetic gas; And regulate the amount of adding the sulphur in carbonaceous material to based on the sulphur concentration that detects and be maintained at about 0.1vol% or higher with the sulphur concentration with in synthetic gas.

13. the 12nd section described method, described method also comprise when the sulphur concentration in synthetic gas when 0.1vol% is following, increase the amount of adding the sulphur in carbonaceous material to.

14. the 12nd or 13 section described method, described method also comprise when the sulphur concentration in synthetic gas when 0.4vol% is above, reduce the amount of adding the sulphur in carbonaceous material to.

15. a method that is used for keeping the synthetic gas sulphur concentration, described method comprises: sulphur is added to the speed of controlling the carbonaceous mixture that comprises sulphur in carbonaceous material with generation, wherein said the first feeder is regulated the speed of the sulphur of controlling; The carbonaceous mixture that will comprise sulphur is incorporated in feed system and comprises the sulphur carbonaceous feed with generation; The carbonaceous feed that will comprise sulphur is incorporated in gasifier, and described gasifier is that approximately 0.1vol% extremely approximately operates under the condition of the synthetic gas of 0.4vol% being enough to generate sulphur concentration; Detect the sulphur concentration in synthetic gas; During at the following % of 0.1vol, regulate the first feeder to increase the speed of adding sulphur in carbonaceous material sulphur when sulphur concentration; And when sulphur concentration when 0.4vol% is above, regulate the first feeder to reduce the speed of adding sulphur in carbonaceous material sulphur.

16. the 15th section described method, described method also comprises: the pressure that will comprise the carbonaceous material of sulphur changes to gasifier operation pressure from barometric point.

17. the 15th or 16 section described method, wherein said gasifier approximately 700 ℃ to approximately operating at the temperature of 1,000 ℃.

18. according to any one section described method in the 15th to 17 section, described method also comprises synthetic gas is incorporated in one or more water coolers to generate cooling synthetic gas, wherein after cooling synthetic gas, detects the sulphur concentration of described synthetic gas.

19. the described method of claim 18, described method also comprise, cooling synthetic gas is incorporated in micronized control device partially or even wholly to remove particulate the synthetic gas from cooling, to generate the synthetic gas and the particulate that separates of humble grain; Adopt the second analyzer to detect sulphur concentration in the synthetic gas of humble grain; Sulphur concentration in the synthetic gas of humble grain when first threshold is following, is regulated percentage feeder and is added sulphur in carbonaceous material speed to increase; And the sulphur concentration in the synthetic gas of humble grain is when Second Threshold is above, regulates percentage feeder and adds sulphur in carbonaceous material speed to reduce.

20. according to any one section described method in the 15th to 19 section, wherein said gasifier, operates under the pressure of 500kPa to approximately 2 at about 750kPa.

Used the set of number upper limit and set of number lower limit to describe some embodiment and feature.Should be appreciated that except as otherwise noted, from any lower limit to the scope of any lower limit, all expect.Some lower limit, the upper limit and scope appear in following one or more claim.All numerical value are designated value " approximately " or " approximately " value, and the desired experimental error of those of ordinary skills and variation are taken into account.

Various terms have below been defined.On the degree of the above undefined term that uses in the claims, should provide the most wide in range definition that the technician of this term in association area reflected in the patent as the publication at least one printing or mandate provided.In addition, all patents of quoting in this application, test procedure and other file are incorporated herein by reference fully, and the degree of introducing is that the disclosure content and this application do not have inconsistent and for all compasss of competency that wherein allow this introducing.

, although preamble is for embodiment of the present disclosure, under the prerequisite that does not deviate from base region of the present disclosure, can expect other and further embodiment of the present disclosure, and described the scope of the present disclosure is determined by following claim.

Claims

1. method that be used for to keep the sulphur concentration of synthetic gas, described method comprises:

Sulphur and carbonaceous material are made up to generate the carbonaceous feed that comprises sulphur;

Make at least a portion of the carbonaceous feed that comprises sulphur gasify to generate synthetic gas;

Detect the sulphur concentration in synthetic gas; And

, based on the sulphur concentration that detects, regulate the amount of the sulphur that makes up with carbonaceous material.

2. method claimed in claim 1, wherein said carbonaceous material comprises coal, coke, oil, biomass or their arbitrary combination.

3. method claimed in claim 1, the sulphur concentration of wherein said synthetic gas is 0.1vol% at least.

4. method claimed in claim 1, the mean particle size of wherein said carbonaceous material is approximately 50 microns to approximately 500 microns.

5. method claimed in claim 4, the mean particle size of wherein said sulphur is approximately 50 microns to approximately 500 microns.

6. method claimed in claim 1, wherein use vapor-phase chromatography, spectrometry, vapor-phase chromatography, gas-liquid partition chromatography or their combine detection sulphur.

7. method claimed in claim 6, the wherein said mean particle size that comprises the carbonaceous mixture of sulphur is approximately 400 microns or less.

8. method claimed in claim 1, the wherein said carbonaceous feed that comprises sulphur gasifies in the transportation gasifier.

9. method claimed in claim 1, the wherein said carbonaceous feed that comprises sulphur gasifies in fluidized-bed gasifier.

10. method claimed in claim 1, the wherein said carbonaceous feed that comprises sulphur gasifies in entrained flow gasifiers.

11. method claimed in claim 1, the wherein said carbonaceous feed that comprises sulphur gasifies in fixed bed gasifiers.

12. a method that is used for the sulphur concentration of maintenance synthetic gas, described method comprises:

Sulphur is added to the carbonaceous feed that comprises sulphur in carbonaceous material with generation, described carbonaceous feed comprises the sulphur of 0.05vol% at least;

The carbonaceous feed that will comprise sulphur is incorporated in the transportation gasifier to generate synthetic gas;

Detect the sulphur concentration in synthetic gas; With

Regulate the amount of adding the sulphur in carbonaceous material to based on the sulphur concentration that detects and be maintained at about 0.1vol% or higher with the sulphur concentration with in synthetic gas.

13. the described method of claim 12, described method also comprise, when the sulphur concentration in synthetic gas, when 0.1vol% is following, increase the amount of adding the sulphur in carbonaceous material to.

14. the described method of claim 12, described method also comprise when the sulphur concentration in synthetic gas when approximately 0.4vol% is above, reduce the amount of adding the sulphur in carbonaceous material to.

15. a method that is used for keeping the synthetic gas sulphur concentration, described method comprises:

Sulphur is added to the speed of controlling the carbonaceous mixture that comprises sulphur in carbonaceous material with generation, wherein the first feeder is regulated the speed of the control of sulphur;

The carbonaceous mixture that will comprise sulphur is incorporated in feed system and comprises the sulphur carbonaceous feed with generation;

The carbonaceous feed that will comprise sulphur is incorporated in gasifier, and described gasifier operates being enough to generate under the condition of synthetic gas;

Detect the sulphur concentration in synthetic gas;

, regulate described the first feeder and add sulphur in carbonaceous material speed to increase when 0.1vol% is following when sulphur concentration; With

, regulate described the first feeder and add sulphur in carbonaceous material speed to reduce when 0.4vol% is above when sulphur concentration.

16. the described method of claim 15, described method also comprises: the pressure that will comprise the carbonaceous material of sulphur changes to gasifier operation pressure from barometric point.

17. the described method of claim 15, wherein said gasifier approximately 700 ℃ to approximately operating at the temperature of 1,000 ℃.

18. the described method of claim 15, described method also comprise, described synthetic gas is incorporated in one or more water coolers to generate cooling synthetic gas, wherein after synthetic gas is cooled, detects the sulphur concentration in synthetic gas.

19. the described method of claim 18, described method also comprises:

Cooling synthetic gas is incorporated in the particulate control device partially or even wholly to remove particulate the synthetic gas from cooling, to generate the synthetic gas and the particulate that separates of humble grain;

Adopt the second analyzer to detect sulphur concentration in the synthetic gas of humble grain;

, regulate percentage feeder and add sulphur in carbonaceous material speed to increase when first threshold is following when the sulphur concentration of the synthetic gas of humble grain; With

, regulate percentage feeder and add sulphur in carbonaceous material speed to reduce when Second Threshold is above when the sulphur concentration of the synthetic gas of humble grain.

20. the described method of claim 15, wherein said gasifier, operates under the pressure of 500kPa to approximately 2 at about 750kPa.