CN102888252A - Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology - Google Patents
Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology Download PDFInfo
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Abstract
The invention relates to saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology, which comprises the following steps: feeding gas-liquid-separated crude gas into a saturation tower after removing impurity from the crude gas; completing the saturation tower with medium-pressure overheat steam from a pipe network after increasing humidity and temperature of the interior of the saturation tower; increasing the temperature and the humidity again; dividing into two strands, namely a first strand and a second strand, wherein the volume of the first strand is equal to 20-40% of the total volume; feeding the first strand into an isothermal transformation furnace so as to process depth transformation reaction; mixing transformed mixing gas of the isothermal transformation furnace with the second strand of the crude gas so as to feed into a gas-liquid mixer; after increasing the humidity of the medium-pressure boiler water from a boundary area so as to feed into a first heat isolating transformation furnace, and continuously processing the transformation reaction. Compared with the prior art, saturation tower series/isothermal furnace CO transformation technology solves a series of problems of long saturation hot water tower high moisture rate CO transformation technology procedure, too many heat isolation reaction grade, large system pressure drop, high equipment investment, easy over-temperature transformation furnace, short catalyst service life and the like.
Description
Technical field
The present invention relates to a kind of CO conversion process, specifically refer to a kind of saturator constant-temperature oven string heat insulation furnace CO conversion process.
Background technology
China has successively introduced the large-scale coal chemical engineering equipment that more than ten covers adopt the Shell Coal Gasification techniques beginning of this century, and this technology requires to ature of coal that active principle is high in low, the synthetic gas, working cost is low and environmental friendliness.The crude synthesis gas that Shell Coal Gasification generates adopts the waste heat boiler cooling, and CO butt volume content is up to more than 60% in the crude synthesis gas, and the water vapour volume content is less than 20% simultaneously, and crude synthesis gas has water vapour content and hangs down and the high distinguishing feature of CO content.
China is when introducing the Shell Coal Gasification technology, and this technology commercial operation only limits to use the crude synthesis gas gas combustion-gas vapor combined cycle device after the purification, does not need to arrange the CO shift conversion step.But the Shell Coal Gasification technology is used for just facing when gas making comes the device such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol a high concentration CO converter technique difficult problem.So the introduction of Shell Coal Gasification technology, has also promoted the development and progress of China's high concentration CO converter technique simultaneously greatly.
The CO conversion be water vapour and CO etc. the mole strong exothermal reaction, generate carbonic acid gas and hydrogen.For the crude synthesis gas that different Coal Gasification Technology generates, the chemical reaction process of shift conversion step all is identical, but shift process need to design targetedly according to the characteristics of crude synthesis gas.For the crude synthesis gas that Technology of Shell Coal Gasification generates, when shift conversion step carried out the CO transformationreation, the Focal point and difficult point of shift process design was the bed temperature of effectively controlling the CO transformationreation, prolongs the work-ing life of transformation catalyst.
At present domesticly generally adopt adiabatic shift converter in the design of high concentration CO shift process, transformationreation is strong exothermic process in view of CO, and existing conversion process process organization all adopts the multistage insulation shift converter to react, the intersegmental heat of reaction of removing.The series of problems such as therefore, cause that existing high concentration CO converter technique shift converter is many, calorific loss is large, the easy overtemperature of the first shift converter, catalyst life are short.
It is 201110260539.7 Chinese invention patent application disclosed " a kind of high water-gas ratio saturated hot-water tower share split CO conversion process " such as application number, this high water-gas ratio saturated hot-water tower share split CO conversion process all adopts adiabatic shift converter, reaction order is more, system pressure drop is large, and the rear system energy consumption that compression consumes to conversion gas is high; Especially the first shift converter adopts adiabatic shift converter, and the conversion gas of High Temperature High Pressure will be born in the furnace wall, causes the equipment wall thickness large, and facility investment is high; And the first shift converter catalyzer is in for a long time under the comparatively high temps and moves, and running environment is harsh, and catalyst life is shorter, changes frequently, and process cost is high; Simultaneously, the first shift converter adopts heat insulation furnace, and temperature control is difficulty, overtemperatute easily occurs, and safe operation causes disadvantageous effect to shift conversion step, has potential safety hazard.Because adiabatic reaction progression is many, complicated to the catalyst vulcanization process when shift conversion step is driven, drive length consuming time, expense of shift conversion step is high.
Summary of the invention
Technical problem to be solved by this invention is that the present situation for prior art provides a kind of saturator constant-temperature oven string heat insulation furnace CO conversion process, with the series of problems such as solve existing saturated hot-water tower height water-gas ratio CO conversion process long flow path, adiabatic reaction progression is more, system pressure drop is large, and facility investment is high, the easy overtemperature of shift converter, catalyst life are short.
The present invention solves the problems of the technologies described above the technical scheme that adopts: this saturator constant-temperature oven string heat insulation furnace CO conversion process is characterized in that comprising the steps:
The raw gas of being sent here by coal gasification workshop section is at first sent into gas-liquid separator and is carried out liquid phase and separate;
After sending into the detoxification groove and remove impurity in the raw gas by gas-liquid separator top raw gas out, send in the saturator;
Raw gas is sent into saturator by the bottom of saturator, and the process recycled water of sending from hot-water tower bottom is through behind heat exchange to 190～210 ℃, enters saturator by the top of saturator, and the countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator; The process recycled water of sending bottom saturator is back to hot-water tower after the pressurization of saturator column bottoms pump;
Raw gas is humidified temperature raising in saturator after, sent by the saturator top, after the heat exchange temperature raising, fully mixed with the middle pressure superheated vapour from pipe network again, the temperature raising humidification is divided into two strands subsequently again, namely first strand and second strand, first strand volume is that 20～40%, first strand of cumulative volume sent into the isothermal shift converter and carried out depth conversion reaction, and control enters that the water of the raw gas of isothermal shift converter/dry gas mol ratio is 0.9～1.2,250～280 ℃ of temperature;
The conversion gas mixture that goes out the isothermal shift converter is with after second strand of raw gas mixes, enter in the gas liquid mixer, behind medium pressure boiler water humidification by mixing of gas from the battery limit (BL), send into the first adiabatic shift converter and continue transformationreation, control enters that the mixing air water of the first adiabatic shift converter/dry gas mol ratio is 0.55～0.65,230～250 ℃ of temperature;
Go out one of the first adiabatic shift converter and become gas mixture after heat exchange is cooled to 200～220 ℃, send into the second adiabatic shift converter and proceed transformationreation;
Go out two of the second adiabatic shift converter and become gas mixture after heat exchange is cooled to 180～200 ℃, sent in the hot-water tower by the hot-water tower bottom, carrying out countercurrent mass transfer with the process recycled water that enters from the hot-water tower middle part conducts heat, spray into purification process phlegma and medium pressure boiler water on the top of hot-water tower, the mol ratio of process recycled water and purification and condensation liquid and medium pressure boiler water is 7.0～10.0, carrying out countercurrent mass transfer conducts heat, conversion gas mixture after the hot-water tower top obtains lowering the temperature obtains process recycled water in the hot-water tower bottom.
The consumption of the above-mentioned process recycled water that enters from the hot-water tower middle part is 4.0～6.0 with the mol ratio that enters the butt raw gas of gas-liquid separator.
Employed isothermal shift converter can use any one isothermal shift converter of the prior art in the above-mentioned technique.Preferably, described isothermal shift converter comprises body of heater, be provided with the heat-exchanging tube bundle that is formed by many heat transfer tubes in the described body of heater, described body of heater top is provided with reaction gas entrance and inspection manhole, the upper portion side wall of body of heater is provided with cooling water outlet, bottom of furnace body is provided with conversion gas outlet and cooling water inlet, and the center of described body of heater is provided with gas trap; It is characterized in that described body of heater comprises top first paragraph body of heater and the bottom second segment body of heater that removably connects, the cylindrical shell that is provided with tubular structure in the described second segment body of heater consists of the gas distributor of Reaktionsofen, the upper/lower terminal of this cylindrical shell is connected on upper tubesheet and the lower tubesheet, the inwall interval of described upper tubesheet and described body of heater is gapped, the be tightly connected internal perisporium of described body of heater of the periphery of described lower tubesheet; The top of described upper tubesheet is provided with upper cover, the below of described lower tubesheet is provided with lower cover, described heat-exchanging tube bundle is arranged in the described cylindrical shell, and the two ends of each described heat transfer tube are separately fixed on the described upper and lower tube sheet and are communicated with respectively the cavity that is made of upper cover and upper tubesheet, lower cover and lower tubesheet; The upper end of described gas trap connects described upper tubesheet, and the cavity that described lower cover is positioned at lower cover and described bottom of furnace body formation is passed in the lower end of gas trap; Described upper cover is provided with cooling water outlet, and this cooling water outlet connects described cooling water outlet by rising pipe, and described rising pipe comprises the two portions that are detachably connected; Described lower cover is provided with the cooling water inlet, and this cooling water outlet connects described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two portions that are detachably connected; Be provided with evenly and at intervals a plurality of pores on the described gas distributor.
Preferably, can connect by flange between first paragraph body of heater and the second segment body of heater, body of heater can be supported on vertical placement on the skirt.
In order to make things convenient for the filling of catalyzer, described gas distributor can comprise a plurality of segmentations that are detachably connected, and each segmentation is removably connected by two semicircular cylinders again and consists of.
Further, distributing homogeneity when guaranteeing that gas enters beds, each described segmentation includes outer cylinder body and is set in the interior inner barrel of described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected and forms the inner core be set in the described urceolus, and described outer cylinder body and described inner barrel interval are gapped.Inner barrel plays the effect of quadratic distribution to reaction gas.
Preferably, the density of the pore described in the such scheme on the inner core is greater than described urceolus, and the aperture of the pore on the described endoporus is less than or equal to 3mm.
Consider the settlement issues of catalyzer in the production process, described gas distributor is not offered pore near described upper tubesheet 100mm with interior position, refluxes and short circuit to prevent the reaction gas that catalyst sedimentation causes.
In above-mentioned each scheme, the part that described gas trap exposes to described lower cover is horn-like, and the middle part of described gas trap lower end port is provided with baffle plate, is separated with the space of flowing out for synthetic gas between the periphery of described baffle plate and described gas trap lower end port.The Diffusion of gas stream that this structure can be used gas trap flows, avoided air-flow directly to impact the impact injury that the body of heater lower cover causes body of heater, and can use short stay in the cavity of gas between lower cover and body of heater of gas trap, guaranteed the inside and outside pressure equilibrium of lower cover, and can make the inside and outside envrionment temperature of body of heater and cylindrical shell and lower cover relative even, can not produce stress concentration.
Can be welded to connect by bearing rib between baffle plate and the gas trap, and strengthen by gusset.Preferably, the collection tube top is near not perforate in the upper tubesheet 100mm, refluxes and short circuit to prevent the catalyst sedimentation gas that induces reaction.
Consider the thermal expansion of gas trap, can be provided with adapter sleeve at the lower surface of described upper tubesheet, it is interior and gapped with described upper tubesheet interval that the upper end of described gas trap is positioned at this adapter sleeve, but this gap supplied gas collector thermal expansion.
Consider the thermal expansion of Reaktionsofen inside, can expansion joint be set at described rising pipe, to solve internal-response entire system thermal expansion problem.
The mode of connection of lower tubesheet and body of heater can have multiple, preferably, can be provided with retaining ring at the perisporium of described body of heater, and the upper surface of this retaining ring is provided with annular recesses; Described lower tubesheet is provided with the annular lug suitable with described groove, and described projection is contained in the described groove, and is provided with sealing-ring between projection and the groove.
The internal perisporium of described body of heater is provided with many group strongbacks, every group of strongback comprises left strongback and the right strongback that left and right interval arranges, accordingly, the sidewall of described upper tubesheet is provided with the polylith preset pieces, and each described preset pieces is contained between the corresponding left strongback and right strongback.
Preferably, be welded with 4 preset piecess on the upper tubesheet, cooperate radial location with 4 groups of strongbacks on being welded on inboard wall of furnace body, with being sealed and matched of the Fast Installation that guarantees inner tube bank and described tongue and groove.
Isothermal shift converter in the such scheme adopts overall diameter to the Z-type structure on the whole, the reaction gas upper entering and lower leaving, it is beds between heat transfer tube, walk recirculated cooling water in the pipe, water coolant absorbs conversion heat, according to the requirement of strength that reaction heat shifts out, cooling water circulation process can be that natural circulation also can be pump circulation, and the recirculated cooling water downstream can arrange drum byproduct steam recovery waste heat.Keep the constant of transformationreation temperature by the controlled circulation water yield.
Compared with prior art, the invention has the advantages that:
1, depth conversion adopts constant-temperature oven, and system pressure drop is little, and the compression work of system has reduced energy consumption after saving.
2, isothermal shift converter service temperature is low, and catalyzer running environment is gentle, the catalyzer long service life, and shift conversion step is easily realized long-period stable operation.
3, the self-produced steam of shift conversion step overheated through heat insulation furnace after, all for the transformationreation of self, saved part sect heat-exchanger and energy recovery equipment, simplified technical process, saved facility investment.
4, employed isothermal shift converter in the preferred version, utilize overall diameter to the little characteristics of gas reactor pressure drop, inner reactive system is adopted the equipment self-weight sealing, and the water coolant inlet/outlet pipe is connected with body of heater and is adopted flange to connect, the internal-response system can wholely be extracted out, and the demountable structure of gas distributor is that the quick loading and unloading of catalyzer and the checking maintenance of post facility facilitate in addition.
5, the setting of internal-response systemic circulation cooling water outlet expansion joint and gas-collecting pipe top cover cylinder gap location, take into full account the high temperature stress operating mode, solved the overall thermal expansion of internal-response system and the differential expansion of gas-collecting pipe, be conducive to stable equipment operation and increase the service life.
6, the isothermal shift converter adopts overall diameter to structure, and circulation area is large, and bed resistance is little, and pressure drop is little.Gas distributor adopts inside and outside barrel structure, to the reaction gas quadratic distribution, make gas distribution more even, be conducive to improve transformation efficiency, simultaneously, take into full account the catalyst sedimentation problem, all be reserved with not aperture area of 100mm at gas distributor and collection tube top, can prevent backflow, the short circuit of conversion gas.
7, the present invention adopts shell and tube-type reactor, and between the catalyst loading heat transfer tube, reaction bed temperature is stable, and the life-span is long, and can increase CO conversion gas treatment capacity by increasing gas distributor hop count mode, is conducive to the maximization of device.
Description of drawings
Fig. 1 is the floor map of isothermal shift converter assembly structure in the embodiment of the invention;
Fig. 2 is upper tubesheet location schematic diagram in the embodiment of the invention;
Fig. 3 is lower tubesheet location schematic diagram in the embodiment of the invention;
Fig. 4 is gas distributor structural representation in the embodiment of the invention;
Fig. 5 be along A-A among Fig. 4 to sectional view.
Fig. 6 is gas trap structural representation in the embodiment of the invention;
Fig. 7 is the process flow diagram of the embodiment of the invention.
Embodiment
Following accompanying drawing embodiment is in conjunction with adopting Shell Coal Gasification gas making to produce the typical chemical fertilizer plant of 520,000 ton/years of urea of 300,000 ton/years of synthetic ammonia, the present invention being described in further detail.
To shown in Figure 6, employed isothermal shift converter 5 comprises in the present embodiment such as Fig. 1:
Body of heater 51, comprise main body 511, upper cover 515 and lower cover 512, be provided with transition section 518 between main body 511 and the upper cover 515, the employing flange removably connects between main body 511 and the transition section 518, is between main body 511 and lower cover 512, upper cover 515 and the transition section 518 to be welded to connect.Upper cover 515 tops are provided with reaction gas entrance 516 and top inspection manhole 517, transition section 518 sidewalls are provided with circulating cooling water out 514, main body 511 lower end sidewalls are provided with bottom inspection manhole 513, the lower cover bottom is provided with cooling water inlet 519 and conversion gas outlet 5110, body of heater 51 bottoms are seated on the skirt 56, and skirt 56 is the base for supporting of this isothermal shift converter.
The internal-response system mainly is comprised of parts such as heat-exchanging tube bundle 52, gas distributor 53, gas-collecting pipe 54, oval upper cover 526 and spherical lower covers 522.Upper cover 526 tops are provided with the cooling water outlet pipe 525 that is connected with above-mentioned circulating cooling water out 514, and the rising pipe vertically middle part of part is provided with expansion joint, and the effect of expansion joint is to eliminate the stress that the rising pipe thermal expansion produces; The horizontal component of rising pipe is divided into two sections, and these two sections are detachably connected by flange.Circular lower cover 522 is provided with the internal overhaul manhole 521 that communicates with above-mentioned bottom inspection manhole 513 and the recirculated cooling water import pipeline section that is connected with above-mentioned cooling water inlet 519 flanges.The internal-response system also comprises upper tubesheet 527 and lower tubesheet 5210, and upper tubesheet 527 relies on four preset piecess 5211 that are welded on the upper tubesheet and the four groups of strongbacks 5212 that are welded on the equipment barrel to cooperate radial locations, guarantees axial displacement.Every group of strongback comprises that between left and right every the left strongback and the right strongback that arrange, preset pieces is between the left and right strongback of correspondence.Be welded with retaining ring 5215 on the internal perisporium of main body 511, the upper surface of this retaining ring is provided with annular recesses; The bottom of retaining ring is provided with 16 uniform bearing ribs 5213, and these bearing ribs are welded on main body 511 and the retaining ring 5215, to strengthen the load-bearing of retaining ring; Eight jackscrews 5214 also are set on the retaining ring, make things convenient for the dismounting of reactive system.Lower tubesheet 5210 is provided with the annular lug suitable with groove, and projection is contained in the groove, and is provided with sealing-ring 5217 between projection and the groove.Also be welded with four locating cones 5216 between the inwall of the upper surface of retaining ring and main body 511, locating cone inclination at 45 °; The effect of locating cone mainly is for lower tubesheet is located.Be equipped with the pore that plugs for each heat transfer tube 528 on the upper and lower tube sheet, the two ends of each heat transfer tube are plugged in respectively and form heat-exchanging tube bundle in the corresponding pore, be filled with catalyzer in each heat transfer tube gap, the middle part of heat-exchanging tube bundle is provided with a plurality of strut members 529 for supporting heat-exchanging tube bundle.
As shown in Figure 7, the CO conversion process of the present embodiment is as follows:
160 ℃ of the raw gas temperature of the saturated water vapour of being sent here by coal gasification workshop section, pressure 3.7Mpa, with pipeline raw gas is being delivered to the process of conversion section because calorific loss from gasification workshop section, a small amount of water vapour in raw gas generation phlegma that can be condensed, the coexistence in tubing system of raw gas and lime set can cause corrosion and the vibrations of pipeline and equipment, so raw gas at first needs lime set is wherein separated.
Therefore the present embodiment is sent into raw gas first gas-liquid separator 1, and liquid flows out from the outlet at bottom of gas-liquid separator 1.Out the raw gas through behind the separatory is sent into detoxification groove 2 and is removed the impurity such as ash content the raw gas and heavy metal from gas-liquid separator 1 top, then enters the bottom of saturator 3.
Raw gas carries out heat and mass with the process recycled water counter current contact that from hot-water tower 13 temperature is 190 ℃～200 ℃ in saturator 3, go out the process recycled water of saturator 3 bottoms through 4 pressurizations of saturator column bottoms pump, send again heating cycle use of hot-water tower 13 back to, extract simultaneously 3%～8% of technological cycle water inventory out and go to rear system to carry out stripping, prevent that objectionable impurities from accumulating in the technological cycle water system.Crude synthesis gas is humidified temperature raising in saturator 3, temperature reaches 185 ℃～190 ℃, water/dry gas mol ratio is 0.58～0.62, lift temperature to 205 ℃～210 ℃ through crude synthesis gas well heater 9, sneak into the 4.0Mpa from methanation and steam pipe system, press superheated vapour in 400 ℃, regulate crude synthesis gas water/dry gas mol ratio and be 0.9～1.1, temperature is to be divided into two strands after 250 ℃, namely first strand and second strand, first strand volumetric flow rate is that 30%, the first strand of total flux enters from isothermal shift converter entrance 516 and carries out deep reaction the isothermal shift converter 5.Water coolant in the heat transfer tube 528 that the reaction liberated heat is arranged in the reactor absorbs, become vapour phase after the heat absorption of part water coolant, gas-liquid two-phase returns in the drum 6 by circulating cooling water out 514, carrying out liquid phase in drum 6 separates, it is overheated that isolated gas phase middle pressure steam demethanization operation is carried out, isolated liquid phase relies on gravity to flow out together with the medium pressure boiler water that fills into from drum 6 bottoms, reenter the interior absorption transformationreation of isothermal shift converter heat transfer tube 528 institute liberated heat by cooling water inlet 519.The isothermal shift converter heat transfer tube 528 interior gas-liquid two-phase fluids that produce and the water coolant that reenters are finished circulation by thermal siphon, have saved power consumption.
Be about 260 ℃ from the conversion gas outlet 5110 isothermal conversion gas temperature that go out isothermal shift converter 5, CO butt volume content is about 2.0%～3.0%, the isothermal conversion gas mixes with another strand crude synthesis gas, enter in the gas liquid mixer 7, with fully mix from the 4.0Mpa of battery limit (BL), 130 ℃ of medium pressure boilers feedwater, carry out the Quench humidification, adjusting mixture temperature to 230 ℃, water/dry gas mol ratio is 0.58～0.60, enters the adiabatic shift converter 8 of 1# and continues transformationreation.
A change mixture temperature that goes out the adiabatic shift converter 8 of 1# is about 350 ℃～355 ℃, and CO butt volume content is about 5.0%～5.5%.One change gas mixture enters crude synthesis gas well heater 9 successively, conversion gas water cooler 10 is cooled to 200 ℃ with crude synthesis gas, process recycled water heat exchange, enters the adiabatic shift converter 11 of 2# and proceeds transformationreation.
The two change mixture temperatures that go out the adiabatic shift converter 11 of 2# are about 230 ℃～235 ℃, CO butt volume content is about 1.0%～1.5%, two become gas mixtures enters conversion gas aftercooler 12 and is cooled to 185 ℃ with process recycled water heat exchange from hot-water tower 13, enters hot-water tower 13 bottoms.
Two become gas mixtures at hot-water tower 13 middle parts and process recycled water countercurrent heat-transfer mass transfer from saturator 3, hot-water tower 13 tops with from the process condensate of rear system and the medium pressure boiler feedwater countercurrent heat-transfer mass transfer that replenishes.The technological cycle water temp of being sent by hot-water tower 13 bottoms is 167 ℃, through 14 pressurizations of hot-water tower column bottoms pump, lifts temperature to 195 ℃ through conversion gas aftercooler 12 and conversion gas water cooler 10 successively, sends into saturator 3 tops.The conversion gas temperature of being sent by hot-water tower 13 tops is about 160 ℃, sends into downstream section and reclaims low temperature exhaust heat.
Isothermal shift converter 5 is removed reaction heat by the oiler feed mode, while by-product pressure 4.0Mpa, the middle pressure saturation steam that temperature is 251 ℃, the middle pressure saturation steam of by-product enters drum 6 and separates liquid phase, the middle pressure saturation steam demethanization operation that drum 6 tops are sent is superheated to 400 ℃, then the middle pressure superheated vapour with pipe network becomes in the gas mixture as the additional steam injection of transformationreation together in advance, the liquid phase of drum 6 bottoms enters in the isothermal shift converter 5 by the thermal siphon mode and recycles, fed water to drum 6 interior additional medium pressure boilers by the battery limit (BL) simultaneously, to keep the stable of liquid level of steam drum.
Comparative Examples
For adopting Shell Coal Gasification gas making to produce the typical chemical fertilizer plant of 520,000 ton/years of urea of 300,000 ton/years of synthetic ammonia, enter effective gas (H of conversion section
2+ CO) be approximately 85000Nm
3/ h compares a kind of high water-gas ratio saturated hot-water tower share split CO conversion process and a kind of saturator isothermal string heat insulation furnace CO conversion process significant parameter under this benchmark and sees Table 1.
Table 1
As can be seen from Table 1, in the saturator string constant-temperature oven CO conversion process that the present embodiment provides, shift converter quantity is few, and loaded catalyst is little, hot(test)-spot temperature is low and system pressure drop is less.Can reduce equipment and the catalyzer investment cost of shift conversion step.The low effectively extending catalyst of hot(test)-spot temperature work-ing life, the system pressure drop I with remarkable reduction after the compression work consumption of system, both all can play the purpose of saving process cost.
Claims (10)
1. a saturator constant-temperature oven string heat insulation furnace CO conversion process is characterized in that comprising the steps:
The raw gas of being sent here by coal gasification workshop section is at first sent into gas-liquid separator and is carried out liquid phase and separate;
After sending into the detoxification groove and remove impurity in the raw gas by gas-liquid separator top raw gas out, send in the saturator;
Raw gas is sent into saturator by the bottom of saturator, and the process recycled water of sending from hot-water tower bottom is through behind heat exchange to 190～210 ℃, enters saturator by the top of saturator, and the countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator; The process recycled water of sending bottom saturator is back to hot-water tower after the pressurization of saturator column bottoms pump;
Raw gas is humidified temperature raising in saturator after, sent by the saturator top, after the heat exchange temperature raising, fully mixed with the middle pressure superheated vapour from pipe network again, the temperature raising humidification is divided into two strands subsequently again, namely first strand and second strand, first strand volume is that 20～40%, first strand of cumulative volume sent into the isothermal shift converter and carried out depth conversion reaction, and control enters that the water of the raw gas of isothermal shift converter/dry gas mol ratio is 0.9～1.2,250～280 ℃ of temperature;
The conversion gas mixture that goes out the isothermal shift converter is with after second strand of raw gas mixes, enter in the gas liquid mixer, behind medium pressure boiler water humidification by mixing of gas from the battery limit (BL), send into the first adiabatic shift converter and continue transformationreation, control enters that the mixing air water of the first adiabatic shift converter/dry gas mol ratio is 0.55～0.65,230～250 ℃ of temperature;
Go out one of the first adiabatic shift converter and become gas mixture after heat exchange is cooled to 200～220 ℃, send into the second adiabatic shift converter and proceed transformationreation;
Go out two of the second adiabatic shift converter and become gas mixture after heat exchange is cooled to 180～200 ℃, sent in the hot-water tower by the hot-water tower bottom, carrying out countercurrent mass transfer with the process recycled water that enters from the hot-water tower middle part conducts heat, spray into purification process phlegma and medium pressure boiler water on the top of hot-water tower, the mol ratio of process recycled water and purification and condensation liquid and medium pressure boiler water is 7.0～10.0, carrying out countercurrent mass transfer conducts heat, conversion gas mixture after the hot-water tower top obtains lowering the temperature obtains process recycled water in the hot-water tower bottom.
The consumption of the above-mentioned process recycled water that enters from the hot-water tower middle part is 4.0～6.0 with the mol ratio that enters the butt raw gas of gas-liquid separator.
2. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 1, it is characterized in that described isothermal shift converter comprises body of heater, be provided with the heat-exchanging tube bundle that is formed by many heat transfer tubes in the described body of heater, described body of heater top is provided with reaction gas entrance and inspection manhole, the upper portion side wall of body of heater is provided with cooling water outlet, bottom of furnace body is provided with conversion gas outlet and cooling water inlet, and the center of described body of heater is provided with gas trap; It is characterized in that described body of heater comprises top first paragraph body of heater and the bottom second segment body of heater that removably connects, be provided with gas distributor in the described second segment body of heater, the upper/lower terminal of this gas distributor is connected on upper tubesheet and the lower tubesheet, the inwall interval of described upper tubesheet and described body of heater is gapped, the be tightly connected internal perisporium of described body of heater of the periphery of described lower tubesheet; The top of described upper tubesheet is provided with upper cover, the below of described lower tubesheet is provided with lower cover, described heat-exchanging tube bundle is arranged in the described gas distributor, and the two ends of each described heat transfer tube are separately fixed on the described upper and lower tube sheet and are communicated with respectively the cavity that is made of upper cover and upper tubesheet, lower cover and lower tubesheet; The upper end of described gas trap connects described upper tubesheet, and the cavity that described lower cover is positioned at lower cover and described bottom of furnace body formation is passed in the lower end of gas trap; Described upper cover is provided with cooling water outlet, and this cooling water outlet connects described cooling water outlet by rising pipe, and described rising pipe comprises the two portions that are detachably connected; Described lower cover is provided with the cooling water inlet, and this cooling water outlet connects described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two portions that are detachably connected.
3. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 2 is characterized in that described gas distributor comprises a plurality of segmentations that are detachably connected, and each segmentation is removably connected by two semicircular cylinders again and consists of.
4. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 3, it is characterized in that each described segmentation includes outer cylinder body and is set in the interior inner barrel of described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected and forms the inner core be set in the described urceolus, and described outer cylinder body and described inner barrel interval are gapped.
5. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 4, the density that it is characterized in that the pore on the described inner core are greater than described urceolus, and the aperture of the pore on the described endoporus is less than or equal to 3mm.
6. CO overall diameter according to claim 5 is to the isothermal shift converter, it is characterized in that described gas distributor and gas trap all do not offering pore near described upper tubesheet 100mm with interior position.
7. according to claim 2 to the described saturator constant-temperature oven of 6 arbitrary claims string heat insulation furnace CO conversion process, it is characterized in that the part that described gas trap exposes to described lower cover is horn-like, and the middle part of described gas trap lower end port is provided with baffle plate, is separated with the space of flowing out for synthetic gas between the periphery of described baffle plate and described gas trap lower end port.
8. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 7 is characterized in that the lower surface of described upper tubesheet is provided with adapter sleeve, and it is interior and gapped with described upper tubesheet interval that the upper end of described gas trap is positioned at this adapter sleeve.
9. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 8 is characterized in that described rising pipe is provided with expansion joint.
10. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 9 is characterized in that the perisporium of described body of heater is provided with retaining ring, and the upper surface of this retaining ring is provided with annular recesses; Described lower tubesheet is provided with the annular lug suitable with described groove, and described projection is contained in the described groove, and is provided with sealing-ring between projection and the groove; The internal perisporium of described body of heater is provided with many group strongbacks, every group of strongback comprises upper strongback and the lower strongback that upper and lower interval arranges, accordingly, the sidewall of described upper tubesheet is provided with the polylith preset pieces, and each described preset pieces is contained between the corresponding upper strongback and lower strongback.
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| CN103879961A (en) * | 2014-03-24 | 2014-06-25 | 中石化宁波工程有限公司 | Saturation tower split-circulation CO transformation process |
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Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1522994A (en) * | 1975-09-18 | 1978-08-31 | British Gas Corp | Shift conversion processes |
| US4542114A (en) * | 1982-08-03 | 1985-09-17 | Air Products And Chemicals, Inc. | Process for the recovery and recycle of effluent gas from the regeneration of particulate matter with oxygen and carbon dioxide |
| US5358696A (en) * | 1993-12-01 | 1994-10-25 | Texaco Inc. | Production of H2 -rich gas |
| US6063355A (en) * | 1996-04-23 | 2000-05-16 | Ebara Corporation | Method for treating wastes by gasification |
| US20050188619A1 (en) * | 2004-03-01 | 2005-09-01 | Thomas Rostrup-Nielsen | Process for cooling an exothermic reaction zone and reactor unit |
| US20060230680A1 (en) * | 2002-05-16 | 2006-10-19 | Thomas Rostrup-Nielsen | Carbon monoxide conversion process and reactor |
| CN101050391A (en) * | 2007-03-30 | 2007-10-10 | 青岛联信化学有限公司 | Sulfur resisting transform technique under low water / gas for gasifying powdered coal |
| CN101704513A (en) * | 2009-08-13 | 2010-05-12 | 上海国际化建工程咨询公司 | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof |
| CN101955154A (en) * | 2010-10-25 | 2011-01-26 | 付元波 | Isothermal conversion process method for high-concentration carbon monoxide conversion |
| CN102002403A (en) * | 2010-11-09 | 2011-04-06 | 中国石油化工股份有限公司 | Low water-air ratio and middle water-air ratio carbon monoxide (CO) conversion process |
| CN102337161A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process |
| CN102337159A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Saturated hot water tower high-water-steam-ratio CO transformation process |
-
2012
- 2012-10-08 CN CN201210378121.0A patent/CN102888252B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1522994A (en) * | 1975-09-18 | 1978-08-31 | British Gas Corp | Shift conversion processes |
| US4542114A (en) * | 1982-08-03 | 1985-09-17 | Air Products And Chemicals, Inc. | Process for the recovery and recycle of effluent gas from the regeneration of particulate matter with oxygen and carbon dioxide |
| US5358696A (en) * | 1993-12-01 | 1994-10-25 | Texaco Inc. | Production of H2 -rich gas |
| US6063355A (en) * | 1996-04-23 | 2000-05-16 | Ebara Corporation | Method for treating wastes by gasification |
| US20060230680A1 (en) * | 2002-05-16 | 2006-10-19 | Thomas Rostrup-Nielsen | Carbon monoxide conversion process and reactor |
| US20050188619A1 (en) * | 2004-03-01 | 2005-09-01 | Thomas Rostrup-Nielsen | Process for cooling an exothermic reaction zone and reactor unit |
| CN101050391A (en) * | 2007-03-30 | 2007-10-10 | 青岛联信化学有限公司 | Sulfur resisting transform technique under low water / gas for gasifying powdered coal |
| CN101704513A (en) * | 2009-08-13 | 2010-05-12 | 上海国际化建工程咨询公司 | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof |
| CN101955154A (en) * | 2010-10-25 | 2011-01-26 | 付元波 | Isothermal conversion process method for high-concentration carbon monoxide conversion |
| CN102002403A (en) * | 2010-11-09 | 2011-04-06 | 中国石油化工股份有限公司 | Low water-air ratio and middle water-air ratio carbon monoxide (CO) conversion process |
| CN102337161A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Low water-to-gas ratio serial saturation tower and hot water tower CO conversion process |
| CN102337159A (en) * | 2011-08-30 | 2012-02-01 | 中国石油化工股份有限公司 | Saturated hot water tower high-water-steam-ratio CO transformation process |
Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103922278A (en) * | 2013-08-25 | 2014-07-16 | 贵州兴化化工股份有限公司 | Heat recovery method in transformation process |
| CN103881766A (en) * | 2014-03-24 | 2014-06-25 | 中石化宁波工程有限公司 | Chilling cyclic CO (carbon monoxide) transformation process |
| CN103881767A (en) * | 2014-03-24 | 2014-06-25 | 中石化宁波工程有限公司 | Circulating CO shift process of saturation tower |
| CN103879961A (en) * | 2014-03-24 | 2014-06-25 | 中石化宁波工程有限公司 | Saturation tower split-circulation CO transformation process |
| CN103881766B (en) * | 2014-03-24 | 2015-06-10 | 中石化宁波工程有限公司 | Chilling cyclic CO (carbon monoxide) transformation process |
| CN104818065A (en) * | 2015-01-30 | 2015-08-05 | 成都高科达科技有限公司 | Adiabatic cooling type methanation synthesis method for methane |
| CN104818065B (en) * | 2015-01-30 | 2017-03-15 | 成都高科达科技有限公司 | A kind of adiabatic cooling type methanation synthesizing methane method |
| CN107118810A (en) * | 2017-05-05 | 2017-09-01 | 北京清创晋华科技有限公司 | It is a kind of to go out the heating of scrubbing tower synthesis gas except the method for aqueous water |
| CN110240948A (en) * | 2019-06-28 | 2019-09-17 | 中石化南京工程有限公司 | A kind of coal chemical industry temperature control transformation coproduction electrical energy system and method |
| CN110357035A (en) * | 2019-08-29 | 2019-10-22 | 陕西聚能新创煤化科技有限公司 | The total transform system and transform method of coal gasification |
| CN110357040A (en) * | 2019-08-29 | 2019-10-22 | 陕西聚能新创煤化科技有限公司 | Coal gasification methanol transformation system and transform method |
| US11918991B2 (en) | 2019-09-03 | 2024-03-05 | Haldor Topsøe A/S | Reformer furnace with supported reformer tubes |
| CN114173918A (en) * | 2019-09-03 | 2022-03-11 | 托普索公司 | Reformer with supported reformer tubes |
| CN111086972A (en) * | 2019-10-24 | 2020-05-01 | 中石化宁波工程有限公司 | CO isothermal conversion process and isothermal conversion furnace matched with pulverized coal gasification |
| CN111115573A (en) * | 2019-10-24 | 2020-05-08 | 中石化宁波工程有限公司 | Poly-generation isothermal transformation process and isothermal transformation furnace matched with coal water slurry gasification process |
| CN110921621A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Low-steam-ratio poly-generation isothermal transformation process and isothermal transformation furnace matched with pulverized coal gasification |
| CN110898769B (en) * | 2019-10-24 | 2022-06-10 | 中石化宁波工程有限公司 | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace |
| CN111086972B (en) * | 2019-10-24 | 2023-04-07 | 中石化宁波工程有限公司 | CO isothermal conversion process and isothermal conversion furnace matched with pulverized coal gasification |
| CN110921621B (en) * | 2019-10-24 | 2023-04-07 | 中石化宁波工程有限公司 | Low-steam-ratio poly-generation isothermal transformation process and isothermal transformation furnace matched with pulverized coal gasification |
| CN111115573B (en) * | 2019-10-24 | 2023-06-06 | 中石化宁波工程有限公司 | Polygeneration isothermal shift process matched with coal water slurry gasification process and isothermal shift furnace |
| CN110898769A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace |
| CN113460962A (en) * | 2021-07-06 | 2021-10-01 | 中石化宁波工程有限公司 | Long-period transformation process for adjusting water-gas ratio by one-step method for oxo synthesis |
| CN113460962B (en) * | 2021-07-06 | 2022-10-11 | 中石化宁波工程有限公司 | Long-period transformation process for adjusting water-gas ratio by one-step method for oxo synthesis |
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