CN101704513B - Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof - Google Patents
Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof Download PDFInfo
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Abstract
The invention discloses a shunting-type isothermal sulfur-tolerant conversion process. The process comprises the following steps: shunting raw coal gas from exterior into at least two parts; leading overheat stream in the first part of the raw coal gas to increase the temperature to 200-300 DEG C; and then entering a first-stage conversion reaction step to carry out a conversion reaction and generate first conversion gas; and conveying the other part of the raw coal gas to next-stage conversion reaction step to carry out a conversion reaction. The catalyst bed of a shift converter has the advantages of stable temperature, simple control, convenient operation and low output CO content. The invention has the advantages of short conversion flows, few equipment, reduced resistance, great byproduct stream amount, high overheat temperature, stream pressure and heat recovery rate, and the like, thereby achieving the aims of reducing conversion stages, equipment number and resistance fall, decreasing investment, having great byproduct stream amount and high overheat temperature, stream pressure and heat recovery rate, reducing conversion stream consumption and outward wastewater discharge, protecting the environment and easily maximizing the device equipment. The invention also discloses shunting-type isothermal sulfur-tolerant conversion equipment used by the process.
Description
Technical field
The invention belongs to the gas sweetening field, relate to a kind of gas maked coal body that is used for, adopt the wide temperature sulfur-resistant transformation catalyst of Co-Mo, make carbon monoxide and water vapor generation transformationreation generate the shunting-type isothermal sulfur-tolerant conversion process and the equipment of hydrogen and carbonic acid gas.The present invention is applicable to large-scale and ultra-large type changing device such as coal system synthetic natural gas, coal system synthetic oil, coal system alcohol mixture, coal system methyl alcohol.
Background technology
In recent years, the fast development of Coal Chemical Industry preparing synthetic gas, different derived product is to H in the synthetic gas
2The requirement difference of/CO ratio generally adopts transformationreation to adjust gas composition.Carbon monoxide (CO) changing device plays an important role in devices such as coal system synthetic natural gas, coal system synthetic oil, coal system alcohol mixture, coal system methyl alcohol, and the energy consumption of conversion is occupied suitable ratio in the total energy consumption of product.
Conversion process, conversion equipment are innovated, optimized, carbon monoxide content is very high in the particularly at present new coal gasifying process coal gas, in research conversion countermeasure and when reducing steam consumption, recycle high and low potential energy that transformationreation produces as far as possible and be an important goal of the large-scale and ultra-large type coal chemical engineering equipment energy-saving and emission-reduction of modernization.
Traditional CO sulfur resistant conversion process, transformationreation is carried out in adiabatic reactor (shift converter), generally is multi-stage transformation, has following drawback: 1, conversion progression is many, and equipment is many, and resistance drop is big, and investment is big; 2, most of catalyzer is in higher temperature out (being hot(test)-spot temperature substantially) operation, and the life-span is short; 3, overtemperature, temperature runaway appear in temperature of reactor control difficulty easily, and big to shift converter pressure housing and upstream device influence, safe operation causes a hidden trouble to device; 4, catalyst vulcanization process complexity, and the sulfuration overtemperature takes place easily; 5, need the other well heater that goes into operation (naked light or steam heating), so that catalyzer is heated up, vulcanizes and regeneration etc.; 6, owing to be subjected to the influence of thermal insulation warming, reactor outlet CO concentration is restricted by molecular balance, is difficult to the level that reaches lower; 7, reaction temperature rising can make the temperature of reactor exceed the catalyst activity scope, causes the active ingredient clinkering of catalyst surface, and specific surface area descends significantly, active decline, even can't use; 8, the shift converter size is big, the flow process complexity of recovery of heat.
Chinese patent publication number CN1429764A discloses " a kind of CO isothermal sulfur-tolerant conversion process ", this isothermal sulfur resistant conversion process practicality is little by analysis, and there are the following problems: 1, the shell and tube reactor catalyst loading coefficient that adopts in this invention is low, the catalyzer loading amount is few, is not suitable for maximizing and the large device; Built-in coil pipe type reactor is littler than huyashi-chuuka (cold chinese-style noodles), move the heat difficulty, and isoplanar temperature difference is big, causes local superheating easily, is not suitable for the gas reforming of high CO content; 2, adopt one section isothermal conversion to carry out depth conversion, perhaps byproduct steam pressure is low, and heat recovery efficiency is poor; Perhaps steam-to-gas ratio is big, promptly consumes a large amount of steam, produces a large amount of waste water; Adopt two sections or three sections isothermal conversion, equipment is many, system complex, and investment is big; 3, the by-product saturation steam can not use as power steam, and actual recovery of heat effect is bad; 4, do not consider the obstruction problem that shifts out of a large amount of reaction heat of high CO content gas conversion, promptly natural circulation can't realize shifting out of high-throughput heat.
Summary of the invention
One of technical problem to be solved by this invention is to overcome the deficiencies in the prior art, a kind of new CO shunting-type isothermal sulfur-tolerant conversion process is provided, it is by shunting on the flow process, problem such as overheated, the adiabatic shift converter temperature rise that solves the conversion byproduct steam is excessive, steam-to-gas ratio is excessive and wastewater flow rate is excessive.On technology, adopt pump circulation to move by the use of thermal means, solve the heat problem that moves of big thermal discharge, big heat flux,, adapt to the conversion of high CO coal gas to reduce hot(test)-spot temperature.
Two of technical problem to be solved by this invention is to overcome the deficiencies in the prior art, and a kind of new CO shunting-type isothermal sulfur-tolerant conversion equipment is provided, and its adiabatic shift-converter can be axial, also can be a radial; The isothermal shift converter can be axial, also can be a radial; Adopt the big shift converter internals pattern of catalyst loading coefficient, for example shell-and-plate solves the big and equipment enlarging problem of catalyzer loading amount; There is potential safety hazard in the pipe connection that solves shift converter and downstream heat-exchange equipment on pipelining is arranged or invests excessive problem.
Shunting-type isothermal sulfur-tolerant conversion process as first aspect present invention, it is characterized in that, be split into two portions at least from the raw material coal gas that out-of-bounds comes, wherein first part's raw material coal gas is allocated superheated vapour into, enter first step shift-reaction step after temperature is increased to 200-300 ℃ and carry out transformationreation, the output first conversion gas, rest part is admitted to the next stage shift-reaction step and carries out transformationreation.
The volume of described first part raw material coal gas is the 10-40% of the feed coal gas volume that out-of-bounds comes.
Described next stage shift-reaction step comprises a second stage shift-reaction step at least, the rest part unstripped gas is at least also told the second section unstripped gas, and be mixed into second stage shift-reaction step with the first conversion gas and carry out transformationreation, the output second conversion gas.
Described first step shift-reaction step is adiabatic shift-reaction step, the first conversion temperature degree that this first step shift-reaction step is come out is 400-500 ℃, temperature is that 400-500 ℃ the first conversion pneumatic transmission is gone into a vapor superheater and reclaimed heat, and temperature is reduced to 250-350 ℃ the first conversion gas and second section raw material coal gas, and to be mixed into temperature be that 200-300 ℃ of mixed gas sent into second stage shift-reaction step and carried out transformationreation.
Described second stage shift-reaction step is the isothermal shift-reaction step, the second conversion temperature degree that this second stage shift-reaction step is come out is 250-350 ℃, the second conversion pneumatic transmission is gone into a feedwater preheater and is reclaimed heat, isolates final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Press saturation steam among the described isothermal shift-reaction step by-product 2.5-9.0MPaG, should middlely press saturation steam to be adopted pump circulation to move hot mode and send into drum by pump, isolate by this drum and to press saturation steam in the by-product, press saturation steam to be admitted to described vapor superheater in the isolated by-product and be superheated to 350-450 ℃ and send, the boiler feed water of feedwater preheater preheating is admitted to drum.
Described second stage shift-reaction step is adiabatic shift-reaction step, the second conversion temperature degree temperature that second stage shift-reaction step is come out is 400-500 ℃, the boiler feed water that the second conversion pneumatic transmission is gone into after the waste heat boiler preheating interior with entering waste heat boiler carries out sending into feedwater preheater recovery heat after the heat exchange, isolates final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Boiler feed water after the feedwater preheater preheating is sent among the waste heat boiler by-product 2.5-9.0MPaG and is pressed saturation steam, presses saturation steam to be admitted to described vapor superheater in the by-product and is superheated to 350-450 ℃ and sends.
Perhaps described first step shift-reaction step is the isothermal shift-reaction step, the temperature of the first conversion gas that first step shift-reaction step is come out is 250-350 ℃, send into a feedwater preheater and reclaim heat, isolate final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Press saturation steam among the described isothermal shift-reaction step by-product 2.5-9.0MPaG, press saturation steam to be adopted pump circulation to move hot mode in this and send into drum, isolate by this drum and press saturation steam to send in the by-product by pump.
Shunting-type isothermal sulfur-tolerant conversion equipment as second aspect present invention, at least comprise one first shift-converter and a feedwater preheater and recovery of heat cooling system, the first conversion gas outlet pipe of first shift-converter is connected with the feedwater preheater inlet mouth, and the feedwater preheater air outlet is connected with described recovery of heat cooling system; The unstripped gas inlet of first shift-converter connects raw material coal gas.Be split into two portions at least from the raw material coal gas that out-of-bounds comes, wherein first part's raw material coal gas is allocated superheated vapour into, temperature is increased to the unstripped gas inlet that enters after 200-300 ℃ by first shift-converter to enter first shift-converter and carries out transformationreation, the output first conversion gas, rest part is admitted to the next stage shift-converter and carries out transformationreation; The first conversion gas is sent into described recovery of heat cooling system again by pipeline and is isolated conversion gas and condenser after sending into described feedwater preheater recovery heat by the first conversion gas outlet pipe.
In one embodiment of the invention, described shunting-type isothermal sulfur-tolerant conversion equipment also comprises a drum, described first shift-converter is the isothermal shift-converter, described first shift-converter moves thermal loop by a pump circulation that is made of pump and pipeline and is connected with drum, the boiler feed pipe of described feedwater preheater is connected with drum, the oiler feed after drum is carried preheating; First part's raw material coal gas is allocated superheated vapour into, temperature is increased to after 200-300 ℃ unstripped gas inlet by first shift-converter to enter first shift-converter and carries out transformationreation, the output first conversion gas, the first conversion gas is sent into described recovery of heat cooling system again and is isolated conversion gas and condenser after sending into described feedwater preheater recovery heat by the first conversion gas outlet pipe; Press saturation steam in the first shift-converter by-product, press saturation steam to move thermal loop in the by-product and send into drum and separate, press saturation steam to send during described drum is isolated by the steam outlet pipe of drum by pump circulation.
In another embodiment, described shunting-type isothermal sulfur-tolerant conversion equipment also comprises one second shift-converter, a vapor superheater, a drum, wherein first shift-converter is adiabatic shift-converter, second shift-converter is the isothermal shift-converter, wherein the first conversion gas inlet tube of first conversion gas outlet pipe of first shift-converter and vapor superheater is direct, the first conversion letter shoot of vapor superheater is connected with the unstripped gas of second shift-converter inlet, and the unstripped gas inlet of second shift-converter also connects raw material coal gas; Described second shift-converter moves thermal loop by a pump circulation that is made of pump and pipeline and is connected with drum, the second conversion gas outlet pipe of second shift-converter is connected with the feedwater preheater inlet mouth, the boiler feed pipe of described feedwater preheater is connected with drum, the oiler feed after drum is carried preheating; The steam outlet pipe of drum connects the middle pressure saturation steam inlet of vapor superheater, presses superheated vapour during the middle pressure superheated vapour outlet pipe of vapor superheater is sent.First part's raw material coal gas is allocated superheated vapour into, temperature is increased to after 200-300 ℃ unstripped gas inlet by first shift-converter to enter first shift-converter and carries out transformationreation, the output first conversion gas, the first conversion gas is sent into vapor superheater by the first conversion gas outlet pipe, carry out heat exchange with the middle pressure saturation steam of sending into, the middle pressure superheated vapour of vapor superheater output is sent by middle pressure superheated vapour outlet pipe, be delivered to the unstripped gas inlet of second shift-converter by the first conversion letter shoot through the first conversion gas behind the recovery heat, with enter second shift-converter after the raw material coal gas of rest part mixes and carry out transformationreation, the output second conversion gas, the second conversion gas is sent into described recovery of heat cooling system again and is isolated conversion gas and phlegma after sending into described feedwater preheater recovery heat by the second conversion gas outlet pipe of second shift-converter; Press saturation steam in the second shift-converter by-product, pressing saturation steam to move thermal loop by pump circulation in the by-product sends into drum and separates, press saturation steam to deliver to vapor superheater by the steam outlet pipe of drum during described drum is isolated and carry out overheatedly, the middle pressure superheated vapour of vapor superheater output is sent by the middle pressure superheated vapour outlet pipe of vapor superheater.
In another embodiment of the present invention, described shunting-type isothermal sulfur-tolerant conversion equipment also comprises one second shift-converter, a vapor superheater, a waste heat boiler, wherein first shift-converter and second shift-converter are adiabatic shift-converter, wherein the first conversion gas inlet tube of first conversion gas outlet pipe of first shift-converter and vapor superheater is direct, the first conversion letter shoot of vapor superheater is connected with the unstripped gas of second shift-converter inlet, and the unstripped gas inlet of second shift-converter also connects raw material coal gas; The second conversion gas inlet tube of second conversion gas outlet pipe of described second shift-converter and waste heat boiler is direct-connected, the second conversion letter shoot of waste heat boiler is connected with the feedwater preheater inlet mouth, the boiler feed pipe of described feedwater preheater is connected with the admission port of waste heat boiler, the oiler feed after waste heat boiler is carried preheating; The steam outlet pipe of waste heat boiler connects the middle pressure saturation steam inlet of vapor superheater, presses superheated vapour during the middle pressure superheated vapour outlet pipe of vapor superheater is sent.First part's raw material coal gas is allocated superheated vapour into, temperature is increased to after 200-300 ℃ unstripped gas inlet by first shift-converter to enter first shift-converter and carries out transformationreation, the output first conversion gas, the first conversion gas is sent into vapor superheater by the first conversion gas outlet pipe, carry out heat exchange with the middle pressure saturation steam of sending into, the middle pressure superheated vapour of vapor superheater output is sent by middle pressure superheated vapour outlet pipe, be delivered to the unstripped gas inlet of second shift-converter by the first conversion letter shoot through the first conversion gas behind the recovery heat, with enter second shift-converter after the raw material coal gas of rest part mixes and carry out transformationreation, the output second conversion gas, the second conversion gas is sent into described recovery of heat cooling system again and is isolated conversion gas and condenser after sending into described waste heat boiler recovery heat by the second conversion gas outlet pipe of second shift-converter; Press saturation steam in the waste heat boiler by-product, press saturation steam to deliver to vapor superheater by steam outlet pipe in the by-product and carry out overheatedly, the middle pressure superheated vapour of vapor superheater output is sent by the middle pressure superheated vapour outlet pipe of vapor superheater.
Described adiabatic shift-converter is axialmode shift-converter or axle radial mode shift-converter.
Described isothermal shift-converter is a kind of in vertical shell-and-tube, vertical cooling pipe type, vertical board-like, horizontal shell-and-tube, horizontal cooling pipe type, the horizontal board-like isothermal shift-converter.
Owing to adopted technical scheme as above, the present invention compared with prior art has following characteristics:
(1) adopts the shunting flow arrangement on the flow process of the present invention, adiabatic conversion load is determined by the heat request of crossing of byproduct steam, add quantity of steam and satisfy the interconversion rate requirement and satisfy adiabatic conversion control temperature rise requirement, reach and add that quantity of steam is minimum, minimum, the simple purpose of heat recovery scheme of generation wastewater flow rate.
(2) flow arrangement of shunting, solve the problems of excessive heat of conversion byproduct steam, simultaneously with the conversion load on the isothermal shift converter, make the stress minimum that produces on the catalyzer, catalyzer is in comparatively in the demulcent isothermal reaction process, can prolong the work-ing life of catalyzer.
(3) adiabatic reactor adopt axially or the diameter of axle to the shift-converter structure, improve the catalyst loading coefficient, help device and maximize, also reduce the resistance drop of beds simultaneously.
(4) the isothermal shift-converter is a vertical shell-and-tube, vertical cooling pipe type, vertical board-like, horizontal shell-and-tube, horizontal cooling pipe type, a kind of in the horizontal board-like isothermal shift-converter, make the catalyzer of isothermal shift-converter both can be contained between the heat exchanger plates of vertical or horizontal shell-and-plate reactor, also can be contained in the heat transfer tube of vertical or horizontal shell and tube-type reactor, also can be contained in the pressurized vessel of vertical or horizontal cooling pipe type reactor, the purpose that adopts this special isothermal shift-converter structure is the heat that produces in the CO transformationreation process in order to remove fast, thereby reaches the isothermal purpose of beds.Specifically:
For the shell-and-plate reactor, catalyst loading is used to walk oiler feed and steam mixture in the plate between heat exchanger plates.When reaction produces in a large number when hot, the water section of bottom inlet becomes steam, forms the vapour-liquid two-phase in heat exchanger plates.Because the carburetion of water, make the heat that produces in the reaction process to remove by the mode that the oiler feed evaporation produces steam.Pressure basically identical in the whole heat exchanger plates and stable can guarantee that the vaporization temperature of water or vapour-liquid two-phase temperature are constant, realizes the constant of reaction bed temperature thus.
For shell and tube-type reactor, catalyst loading is walked oiler feed and steam mixture outside the pipe in heat transfer tube.When reaction produces in a large number when hot, the water section of bottom inlet becomes steam, forms the vapour-liquid two-phase between pipe.Because the carburetion of water, make the heat that produces in the reaction process to remove by the mode that the oiler feed evaporation produces steam.Pressure basically identical between whole pipe and stable can guarantee that the vaporization temperature of water or vapour-liquid two-phase temperature are constant, realizes the constant of reaction bed temperature thus.
For the cooling pipe type reactor, catalyst loading is walked oiler feed and steam mixture in the pipe between heat transfer tube, and promptly cold pipe is embedded in the beds fully.When reaction produces in a large number when hot, the water section of bottom inlet becomes steam, formation vapour-liquid two-phase in pipe.Because the carburetion of water, make the heat that produces in the reaction process to remove by the mode that the oiler feed evaporation produces steam.Pressure basically identical in the whole pipe and stable can guarantee that the vaporization temperature of water or vapour-liquid two-phase temperature are constant, realizes the constant of reaction bed temperature thus.
(5) the first-class temperature shift reaction device of technology adopts pump circulation to move heat, the medium that is used to remove reaction heat is a water, be so-called oiler feed-steam system, (2.5～9.0MPaG), employing pump pump circulation is thrown oiler feed into the isothermal shift-converter to press superheated vapour in the by-product; Filmwise boiling when pump circulation can be avoided water vapor, promotion shift converter catalyzer move heat rapidly, reduce focus and bed temperature; And because pump circulation, device operational load elasticity is big, and it doesn't matter promptly to move the foundation of thermal cycling and load in the shift converter, and these are different fully with natural circulation.Therefore the present invention is particularly suitable for the conversion of the high unstripped gas of CO content.Leaving the oiler feed of isothermal shift-converter and the vapour-liquid two-phase of steam is connected by the drum of pipeline with isothermal shift-converter outside, vapor-liquid separation in the drum, gas is the middle pressure saturation steam of by-product, and liquid and the oiler feed that replenishes enter shift converter continuation absorption heat together and partly vaporize.Therefore, can be that temperature that the temperature of water evaporation is regulated beds reaches and waits the controlled purpose of gentleness by the pressure of regulating drum, under any operational condition, particularly under driving, underrun and accident conditions, water circulation system can guarantee that reaction bed temperature is stable.
In addition, pump circulation can replenish the fresh oiler feed of part the inlet of recycle pump, promptly can Control Circulation water goes into the temperature of shift converter, changes the temperature of lower part outlet catalyzer, thereby changes the transformationreation balance, further improves interconversion rate.And natural circulation can only all mend drum to oiler feed, and the water temp of going into shift converter is saturated constant, so the steamed restriction of pressure of interconversion rate.
(6) adopt steam to add the oiler feed circulation loop and beds is heated up, do not need extra well heater from the shift converter cold side; Pump circulation can guarantee intensification sulfuration quick and stable.Catalyst vulcanization is simple, rapidly and do not have overheated danger, is difficult for producing the sulfuration overtemperature.
(7) adiabatic shift-converter directly is connected (be similar to ammonia synthesis converter and the direct of downstream heat exchanger is connected) with downstream heat exchanger, and the cancellation connecting tube reduces the design temperature of lower cover and flange, and investment reduces.Solve the safety problem of shift converter overtemperature, temperature runaway problem and outlet conduit simultaneously; The particular design of heat-exchange equipment guarantees the safety problem of interchanger.
(8) advance the small portion coal gas of adiabatic shift-converter, allocate superheated vapour (300～450 ℃) into, satisfy adiabatic shift converter inlet temperature and require (200～300 ℃), interconversion rate to require and adiabatic shift converter control temperature rise requirement; Go out 400～500 ℃ of the conversion temperature degree of adiabatic shift-converter, enter vapor superheater and reclaim heat, satisfy byproduct steam superheated requirement (300～450 ℃), conversion temperature degree reduces (250～350 ℃).
(9) temperature distribution of beds meets the kinetics requirement of conversion thermopositive reaction, and catalyzer is in best working order.
(10) eliminate the restriction to outlet CO concentration of the balance produced by thermal insulation warming, under the same conditions, outlet CO content is starkly lower than traditional adiabatic sulfur-resisting transformation.
(11) thermal insulation or Isothermal Catalyst bed adopt axial (large-scale changing device) or the diameter of axle to (ultra-large type changing device) inner parts structure, reduce the resistance drop of beds.
(12) most of raw material coal gas of conversion gas and shunting mixes, CO concentration in the dilution raw material coal gas; Steam content can satisfy further conversion requirement in the gas of conversion simultaneously.
Sulfur resistant conversion process of the present invention and equipment, the raw gas that can mate different gas making methods generations is as raw material.Gas making method commonly used comprises: residual oil partial oxidation, coal water slurry gasification, dry coal powder gasification, lurgi gasifier or BGL gasification, fluidized-bed gasification or the like.The present invention is particularly suitable for handling the high raw gas conversion of CO content, the raw gas of the high CO content produced of GSP dry coal powder gasification method for example, and butt CO forms and can reach more than 70%.For the low low temperature shift of CO content, the present invention also can be suitable for.
Technology of the present invention and equipment adapt to 200～500 ℃ of sulfur-resisting transformation operating temperature ranges, pressure range 2.0～10.0MPaG, and (v), steam-to-gas ratio is 0～2.0 to process gas hydrogen sulfide content 〉=0.01%.
(H in the outlet conversion gas
2-CO
2)/(CO+CO
2) can be～2 (coal system methanol device or coal system synthetic oil devices), or 2.0～2.5 (coal system alcohol mixture devices), or～3.0 (coal system synthesis of natural device of air), perhaps higher (synthetic ammonia installation or device for producing hydrogen).
The present invention compared with prior art, have the shift converter reaction bed temperature steadily, control is simple, easy to operate, outlet CO content is low; Shift process is short, equipment is few, resistance reduces; Characteristics such as the byproduct steam amount is big, temperature of superheat is high, vapor pressure is high, heat recovery efficiency height.Therefore technology of the present invention and equipment can reach and reduce conversion progression, reduce table of equipment number and resistance drop, reduce investment; The byproduct steam amount is big, temperature of superheat is high, pressure is high, energy-conservation; Reduce the conversion steam consumption, reduce efflux wastewater, environmental protection; The purpose that appliance arrangement maximizes easily.
Description of drawings
Fig. 1 is the schematic flow sheet of the embodiment of the invention 1.
Fig. 2 is the schematic flow sheet of the embodiment of the invention 2.
Fig. 3 is the schematic flow sheet of the embodiment of the invention 3.
Embodiment
For technique means, creation characteristic that the present invention is realized, reach purpose and effect is easy to understand, below in conjunction with concrete diagram, further set forth the present invention.
Referring to Fig. 1, shunting-type isothermal sulfur-tolerant conversion equipment shown in Figure 1 is fit to the gas reforming of high CO content.
This shunting-type isothermal sulfur-tolerant conversion equipment comprises the first shift-converter R1, the second shift-converter R2, vapor superheater H1, drum V1, feedwater preheater H2 and recovery of heat cooling system H3, and the first shift-converter R1 is adiabatic shift-converter of axialmode or the adiabatic shift-converter of axle radial mode.Second shift-converter is a kind of in vertical shell-and-tube, vertical cooling pipe type, vertical board-like, horizontal shell-and-tube, horizontal cooling pipe type, the horizontal board-like isothermal shift-converter.
The first conversion gas outlet pipe 1 of the first shift-converter R1 is direct with the first conversion gas inlet tube 2 of vapor superheater H1, the first conversion letter shoot 3 of vapor superheater H1 is connected with the unstripped gas of second shift-converter R2 inlet 4, and the unstripped gas inlet 4 of the second shift-converter R2 also connects raw material coal gas 5.The second shift-converter R2 moves thermal loop 6 by a pump circulation that is made of pump P1 and pipeline and is connected with drum V1, the second conversion gas outlet pipe 7 of the second shift-converter R2 is connected with the inlet mouth 8 of feedwater preheater H2, the boiler feed pipe 9 of feedwater preheater H2 is connected with drum V1, the oiler feed after drum V1 carries preheating; The steam outlet pipe 10 of drum V1 connects the middle pressure saturation steam inlet 11 of vapor superheater H1, presses superheated vapour during the middle pressure superheated vapour outlet pipe 12 of vapor superheater H1 is sent.The air outlet 13 of feedwater preheater H2 meets recovery of heat cooling system H3.
The technological process of this embodiment is as follows: from raw material coal gas 5 (dry gas or the saturated coal gas) separated into two parts that out-of-bounds comes, the first part's raw material coal gas 51 that accounts for the raw material coal gas 5 volume 10-40% that out-of-bounds come is allocated superheated vapour 121 into, temperature is increased to after 200-300 ℃ unstripped gas inlet 14 by the first shift-converter R1 to enter the first shift-converter R1 and carries out adiabatic transformationreation, the output temperature is 400-500 ℃ the first conversion gas, the first conversion gas is by the first conversion gas outlet pipe 1, the first conversion gas inlet tube 2 is directly sent into vapor superheater H1, carry out heat exchange with the 11 middle pressure saturation steams of sending into that enter the mouth by middle pressure saturation steam, to reclaim heat, the first conversion temperature degree of being sent by the first conversion letter shoot 3 is reduced to 250-350 ℃.The middle pressure superheated vapour of vapor superheater H1 output is sent by middle pressure superheated vapour outlet pipe 12.
Be delivered to the unstripped gas inlet 4 of the second shift-converter R2 by the first conversion letter shoot 3 through the first conversion gas behind the recovery heat, after the raw material coal gas 52 of rest part mixes, formation temperature is that 200-300 ℃ of mixed gas enters the second shift-converter R2 and wait temperature shift reaction, the output temperature is 250-350 ℃ the second conversion gas, and the second conversion gas is sent into feedwater preheater H2 recovery heat by the second conversion gas outlet pipe 7 of the second shift-converter R2 and the inlet mouth 8 of feedwater preheater H2.The second conversion gas after heat recuperation is sent into recovery of heat cooling system H3 by the air outlet 13 of feedwater preheater H2 again and is isolated conversion gas and phlegma.
Press saturation steam among the second shift-converter R2 by-product 2.5-9.0MPaG, pressing saturation steam to move thermal loop 6 by pump circulation in the by-product sends into drum V1 and separates, press saturation steam to deliver to vapor superheater H1 by the steam outlet pipe 10 of drum V1, middle pressure saturation steam inlet 11 during drum V1 is isolated and carry out overheatedly, the temperature of vapor superheater H1 output is that 350-450 ℃ middle pressure superheated vapour is sent by the middle pressure superheated vapour outlet pipe 12 of vapor superheater H1.A middle pressure pot hot steam part of sending can be allocated in first part's raw material coal gas 51.
The raw material coal gas of present embodiment can be the gas making of GSP dry coal powder, and concrete parameter sees Table 1:
Table 1
Present embodiment can also use the BGL coal generating gas, and concrete parameter sees Table 2
Table 2
Embodiment 2
Referring to Fig. 2, shunting-type isothermal sulfur-tolerant conversion equipment shown in Figure 2 is fit to the gas reforming of high CO content.
This shunting-type isothermal sulfur-tolerant conversion equipment comprises the first shift-converter R1, the second shift-converter R2, vapor superheater H1, waste heat boiler H4, feedwater preheater H2 and recovery of heat cooling system H3,
The first shift-converter R1 and the second shift-converter R2 are adiabatic shift-converter of axialmode or the adiabatic shift-converter of axle radial mode.
The first conversion gas outlet pipe 1 of the first shift-converter R1 is direct with the first conversion gas inlet tube 2 of vapor superheater H1, the first conversion letter shoot 3 of vapor superheater H1 is connected with the unstripped gas of second shift-converter R2 inlet 4, and the unstripped gas inlet 4 of the second shift-converter R2 also connects raw material coal gas 5.It is 15 direct-connected that the second conversion gas outlet pipe 7 of the second shift-converter R2 and the conversion gas of waste heat boiler H4 enter the mouth, the conversion gas of waste heat boiler H4 outlet 16 is connected with the inlet mouth 8 of feedwater preheater H2, the boiler feed pipe 9 of feedwater preheater H2 is connected with the water-in 17 of waste heat boiler H4 cold side, the oiler feed after waste heat boiler H4 carries preheating; The steam outlet pipe 18 of waste heat boiler H4 connects the middle pressure saturation steam inlet 11 of vapor superheater H1, presses superheated vapour during the middle pressure superheated vapour outlet pipe 12 of vapor superheater H1 is sent.The air outlet 13 of feedwater preheater H2 meets recovery of heat cooling system H3.
The technological process of this embodiment is as follows: from raw material coal gas 5 (dry gas or the saturated coal gas) separated into two parts that out-of-bounds comes, the first part's raw material coal gas 51 that accounts for the raw material coal gas 5 volume 10-40% that out-of-bounds come is allocated superheated vapour 121 into, temperature is increased to after 200-300 ℃ unstripped gas inlet 14 by the first shift-converter R1 to enter the first shift-converter R1 and carries out adiabatic transformationreation, the output temperature is 400-500 ℃ the first conversion gas, the first conversion gas is by the first conversion gas outlet pipe 1, the first conversion gas inlet tube 2 is directly sent into vapor superheater H1, carry out heat exchange with the 11 middle pressure saturation steams of sending into that enter the mouth by middle pressure saturation steam, to reclaim heat, the first conversion temperature degree of being sent by the first conversion letter shoot 3 is reduced to 250-350 ℃.The middle pressure superheated vapour of vapor superheater H1 output is sent by middle pressure superheated vapour outlet pipe 12.
Be delivered to the unstripped gas inlet 4 of the second shift-converter R2 by the first conversion letter shoot 3 through the first conversion gas behind the recovery heat, after the raw material coal gas 52 of rest part mixes, formation temperature is that 200-300 ℃ mixed gas enters the second shift-converter R2 and carries out adiabatic transformationreation, the output temperature is 400-500 ℃ the second conversion gas, and the second conversion gas is sent into waste heat boiler H4 recovery heat by the second conversion gas outlet pipe 7 of the second shift-converter R2, the conversion gas inlet 15 of waste heat boiler H4.The second conversion temperature degree after heat recuperation is reduced to 250-350 ℃, send into feedwater preheater H2 by the inlet mouth 8 of the conversion gas of waste heat boiler H4 outlet 16, feedwater preheater H2 again and further reclaim heat, further reclaim the second conversion gas behind the heat and send into recovery of heat cooling system H3 by the air outlet 13 of feedwater preheater H2 and isolate conversion gas and phlegma.
Press saturation steam among the waste heat boiler H4 by-product 2.5-9.0MPaG, press saturation steam to be undertaken overheatedly by delivered to vapor superheater H1 by middle pressure superheated vapour outlet pipe 12 in the by-product, the temperature of vapor superheater H1 output is that 350-450 ℃ middle pressure superheated vapour is sent by the middle pressure superheated vapour outlet pipe 12 of vapor superheater H1.A middle pressure pot hot steam part of sending can be allocated in first part's raw material coal gas 51.
In order to meet the requirements of interconversion rate, the second conversion gas can increase the adiabatic shift-converter of one-level again and carry out three grades of conversion behind gas converting heat in addition.
Embodiment 3
Referring to Fig. 3, the gas reforming of low CO content during shunting-type isothermal sulfur-tolerant conversion equipment shown in Figure 3 is fit to.
This shunting-type isothermal sulfur-tolerant conversion equipment comprises the first shift-converter R1, drum V1, feedwater preheater H2 and recovery of heat cooling system H3,
The first shift-converter R1 is a kind of in vertical shell-and-tube, vertical cooling pipe type, vertical board-like, horizontal shell-and-tube, horizontal cooling pipe type, the horizontal board-like isothermal shift-converter.
The first conversion gas outlet pipe 1 of the first shift-converter R1 is connected with the inlet mouth 8 of feedwater preheater H2, and the boiler feed pipe 9 of feedwater preheater H2 is connected with drum V1, the oiler feed after drum V1 carries preheating; The first shift-converter R1 moves thermal loop 6 by a pump circulation that is made of pump P1 and pipeline and is connected with drum V1, and it is overheated to press saturation steam to send to methanation by the steam outlet pipe 10 of drum V1 during drum V1 is isolated.The air outlet 13 of feedwater preheater H2 meets recovery of heat cooling system H3.The unstripped gas inlet 4 of the first shift-converter R1 connects raw material coal gas 5 and middle pressure superheated vapour 121.
The technological process of this embodiment is as follows: allocate superheated vapour 121 into from the raw material coal gas 5 (dry gas or saturated coal gas) that out-of-bounds comes, temperature is increased to after 200-300 ℃ unstripped gas inlet 14 by the first shift-converter R1 to enter the first shift-converter R1 and waits temperature shift reaction, the output temperature is 250-350 ℃ the first conversion gas, and the first conversion gas is sent into feedwater preheater H2 by the inlet mouth 8 of the first conversion gas outlet pipe 1, feedwater preheater H2 and reclaimed heat.The first conversion gas after heat recuperation is sent into recovery of heat cooling system H3 by the air outlet 13 of feedwater preheater H2 again and is isolated conversion gas and phlegma.
Press saturation steam among the first shift-converter R1 by-product 2.5-9.0MPaG, pressing saturation steam to move thermal loop 6 by pump circulation in the by-product sends into drum V1 and separates, it is overheated to press saturation steam to send to methanation by the steam outlet pipe 10 of drum V1 during drum V1 is isolated
More than show and described ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; that describes in the foregoing description and the specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.The claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (11)
1. shunting-type isothermal sulfur-tolerant conversion process, it is characterized in that, be split into two portions at least from the raw material coal gas that out-of-bounds comes, wherein first part's raw material coal gas is allocated superheated vapour into, enter first step shift-reaction step after temperature is increased to 200-300 ℃ and carry out transformationreation, the output first conversion gas, rest part is admitted to the next stage shift-reaction step and carries out transformationreation; Described first step shift-reaction step is adiabatic shift-reaction step, the first conversion temperature degree that this first step shift-reaction step is come out is 400-500 ℃, temperature is that 400-500 ℃ the first conversion pneumatic transmission is gone into a vapor superheater and reclaimed heat, and temperature is reduced to 250-350 ℃ the first conversion gas and second section raw material coal gas, and to be mixed into temperature be that 200-300 ℃ of mixed gas sent into second stage shift-reaction step and carried out transformationreation.
2. shunting-type isothermal sulfur-tolerant conversion process, it is characterized in that, be split into two portions at least from the raw material coal gas that out-of-bounds comes, wherein first part's raw material coal gas is allocated superheated vapour into, enter first step shift-reaction step after temperature is increased to 200-300 ℃ and carry out transformationreation, the output first conversion gas, rest part is admitted to the next stage shift-reaction step and carries out transformationreation; Described first step shift-reaction step is the isothermal shift-reaction step, the temperature of the first conversion gas that first step shift-reaction step is come out is 250-350 ℃, send into a feedwater preheater and reclaim heat, isolate final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Press saturation steam among the described isothermal shift-reaction step by-product 2.5-9.0MPaG, press saturation steam to be adopted pump circulation to move hot mode in this and send into drum, isolate by this drum and press saturation steam to send in the by-product by pump.
3. shunting-type isothermal sulfur-tolerant conversion process as claimed in claim 1 or 2 is characterized in that, the volume of described first part raw material coal gas is the 10-40% of the feed coal gas volume that out-of-bounds comes.
4. shunting-type isothermal sulfur-tolerant conversion process as claimed in claim 3, it is characterized in that, described next stage shift-reaction step comprises a second stage shift-reaction step at least, the rest part unstripped gas is at least also told the second section unstripped gas, and be mixed into second stage shift-reaction step with the first conversion gas and carry out transformationreation, the output second conversion gas.
5. shunting-type isothermal sulfur-tolerant conversion process as claimed in claim 4, it is characterized in that, described second stage shift-reaction step is the isothermal shift-reaction step, the second conversion temperature degree that this second stage shift-reaction step is come out is 250-350 ℃, the second conversion pneumatic transmission is gone into a feedwater preheater and is reclaimed heat, isolates final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Press saturation steam among the described isothermal shift-reaction step by-product 2.5-9.0MPaG, should middlely press saturation steam to be adopted pump circulation to move hot mode and send into drum by pump, isolate by this drum and to press saturation steam in the by-product, press saturation steam to be admitted to described vapor superheater in the isolated by-product and be superheated to 350-450 ℃ and send, the boiler feed water of feedwater preheater preheating is admitted to drum.
6. shunting-type isothermal sulfur-tolerant conversion process as claimed in claim 4, it is characterized in that, described second stage shift-reaction step is adiabatic shift-reaction step, the second conversion temperature degree temperature that second stage shift-reaction step is come out is 400-500 ℃, the boiler feed water that the second conversion pneumatic transmission is gone into after the waste heat boiler preheating interior with entering waste heat boiler carries out sending into feedwater preheater recovery heat after the heat exchange, isolates final conversion gas and phlegma through delivering to the recovery of heat cooling system behind the feedwater preheater recovery heat; Boiler feed water after the feedwater preheater preheating is sent among the waste heat boiler by-product 2.5-9.0MPaG and is pressed saturation steam, presses saturation steam to be admitted to described vapor superheater in the by-product and is superheated to 350-450 ℃ and sends.
7. shunting-type isothermal sulfur-tolerant conversion equipment, it is characterized in that, at least comprise one first shift-converter and a feedwater preheater and recovery of heat cooling system, the first conversion gas outlet pipe of first shift-converter is connected with the feedwater preheater inlet mouth, and the feedwater preheater air outlet is connected with described recovery of heat cooling system; The unstripped gas inlet of first shift-converter connects raw material coal gas; Described shunting-type isothermal sulfur-tolerant conversion equipment also comprises a drum, described first shift-converter is the isothermal shift-converter, described first shift-converter moves thermal loop by a pump circulation that is made of pump and pipeline and is connected with drum, the boiler feed pipe of described feedwater preheater is connected with drum, the oiler feed after drum is carried preheating; Raw material coal gas is allocated superheated vapour into, temperature is increased to after 200-300 ℃ unstripped gas inlet by first shift-converter to enter first shift-converter and carries out transformationreation, the output first conversion gas, the first conversion gas is sent into described recovery of heat cooling system again and is isolated conversion gas and phlegma after sending into described feedwater preheater recovery heat by the first conversion gas outlet pipe; Press saturation steam in the first shift-converter by-product, press saturation steam to move thermal loop in the by-product and send into drum and separate, press saturation steam to send during described drum is isolated by the steam outlet pipe of drum by pump circulation.
8. shunting-type isothermal sulfur-tolerant conversion equipment, it is characterized in that, at least comprise one first shift-converter and a feedwater preheater and recovery of heat cooling system, the first conversion gas outlet pipe of first shift-converter is connected with the feedwater preheater inlet mouth, and the feedwater preheater air outlet is connected with described recovery of heat cooling system; The unstripped gas inlet of first shift-converter connects raw material coal gas; Described shunting-type isothermal sulfur-tolerant conversion equipment also comprises one second shift-converter, a vapor superheater, a drum, wherein first shift-converter is adiabatic shift-converter, second shift-converter is the isothermal shift-converter, wherein the first conversion gas inlet tube of first conversion gas outlet pipe of first shift-converter and vapor superheater is direct, the first conversion letter shoot of vapor superheater is connected with the unstripped gas of second shift-converter inlet, and the unstripped gas inlet of second shift-converter also connects raw material coal gas; Described second shift-converter moves thermal loop by a pump circulation that is made of pump and pipeline and is connected with drum, the second conversion gas outlet pipe of second shift-converter is connected with the feedwater preheater inlet mouth, the boiler feed pipe of described feedwater preheater is connected with drum, the oiler feed after drum is carried preheating; The steam outlet pipe of drum connects the middle pressure saturation steam inlet of vapor superheater, presses superheated vapour during the middle pressure superheated vapour outlet pipe of vapor superheater is sent.
9. shunting-type isothermal sulfur-tolerant conversion equipment, it is characterized in that, at least comprise one first shift-converter and a feedwater preheater and recovery of heat cooling system, the first conversion gas outlet pipe of first shift-converter is connected with the feedwater preheater inlet mouth, and the feedwater preheater air outlet is connected with described recovery of heat cooling system; The unstripped gas inlet of first shift-converter connects raw material coal gas; Described shunting-type isothermal sulfur-tolerant conversion equipment also comprises one second shift-converter, a vapor superheater, a waste heat boiler, wherein first shift-converter and second shift-converter are adiabatic shift-converter, wherein the first conversion gas inlet tube of first conversion gas outlet pipe of first shift-converter and vapor superheater is direct, the first conversion letter shoot of vapor superheater is connected with the unstripped gas of second shift-converter inlet, and the unstripped gas inlet of second shift-converter also connects raw material coal gas; The second conversion gas inlet tube of second conversion gas outlet pipe of described second shift-converter and waste heat boiler is direct-connected, the second conversion letter shoot of waste heat boiler is connected with the feedwater preheater inlet mouth, the boiler feed pipe of described feedwater preheater is connected with the admission port of waste heat boiler, the oiler feed after waste heat boiler is carried preheating; The steam outlet pipe of waste heat boiler connects the middle pressure saturation steam inlet of vapor superheater, presses superheated vapour during the middle pressure superheated vapour outlet pipe of vapor superheater is sent.
10. shunting-type isothermal sulfur-tolerant conversion equipment as claimed in claim 8 or 9 is characterized in that, described adiabatic shift-converter is axialmode shift-converter or axle radial mode shift-converter.
11. as claim 7 or 8 described shunting-type isothermal sulfur-tolerant conversion equipment, it is characterized in that described isothermal shift-converter is a kind of in vertical shell-and-tube, vertical cooling pipe type, vertical board-like, horizontal shell-and-tube, horizontal cooling pipe type, the horizontal board-like isothermal shift-converter.
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