CN102887481B - Low water-gas ratio pre-conversion constant-temperature CO conversion technology - Google Patents
Low water-gas ratio pre-conversion constant-temperature CO conversion technology Download PDFInfo
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Abstract
The invention relates to a low water-gas ratio pre-conversion constant-temperature CO conversion technology which is characterized by comprising the following steps of: performing gas-liquid separation and heat exchange of raw gas, and heating to 190-230 DEG C; removing impurities; adjusting the temperature to 200-220 DEG C and the water/dry gas molar ratio to 0.19-0.23; performing primary conversion in a pre-conversion furnace; adjusting the water-gas ratio of the pre-conversion mixed gas from the pre-conversion furnace again; and performing deep conversion reaction in a constant-temperature furnace. Compared with the prior art, the technology provided by the invention has short conversion flow and low resistance, saves the compression work of the system and reduces the energy consumption; by adopting the constant-temperature conversion furnace to replace at least two levels of heat insulation conversion furnaces, the number of conversion furnaces is reduced, and the equipment investment is saved; and the reaction is easy to control.
Description
Technical field
The present invention relates to CO conversion process, specifically refer to that a kind of low water-gas ratio becomes string isothermal CO conversion process in advance.
Background technology
China is becoming tight by petroleum resources day in recent years affects, and Coal Chemical Industry has proceeded to a fast-developing stage, and China has in succession introduced the bed pulverized coal gasification technology of more than ten cover shell and carried out producing synthesis gas.Technology of Shell Coal Gasification requires to ature of coal that in low, synthetic gas, active principle is high, working cost is low and environmental friendliness.The cooling employing waste heat boiler of this technology crude synthesis gas, in the crude synthesis gas of generation, CO butt volume content is up to more than 60%, and simultaneously water vapour volume content is less than 20%, and crude synthesis gas has the low and high distinguishing feature of CO content of water vapour content.
China is in the time introducing 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 purifying, and does not need to arrange CO shift conversion step.But when being carried out to the devices such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol for gas making, Shell Coal Gasification technology just faces 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.
Shift conversion step be water vapour and CO etc. mole strong exothermal reaction, generate carbonic acid gas and hydrogen.The crude synthesis gas generating for different Coal Gasification Technology, the chemical reaction process of downstream transforms operation is all identical, but shift process need to design targetedly according to the feature of crude synthesis gas.The crude synthesis gas generating for Technology of Shell Coal Gasification, in the time that shift conversion step carries out CO transformationreation, the Focal point and difficult point of shift process design is the bed temperature of effectively controlling CO transformationreation, and work-ing life, the minimizing that extends transformation catalyst converts sum of series facility investment, reduce the Pressure Drop of shift conversion step and save middle pressure steam and power consumption etc.
At present domesticly in the design of high concentration CO shift process, generally adopt adiabatic shift converter, in view of CO, transformationreation is strong exothermic process, and existing conversion process process organization all adopts 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 technical process is long, calorific loss is many, the short and energy consumption of the easy overtemperature of shift converter, catalyzer running environment harshness life-span is high.
As disclosed in the Chinese invention patent application that application number is 200910056342.4 " shunting-type isothermal sulfur-tolerant conversion process and equipment thereof ", there is following problems in this technique:
1, the water/dry gas mol ratio and temperature and the catalyzer air speed parameter that specifically do not define the conversion gas that enters every shift converter, only provided a wide in range temperature and water/dry gas molar ratio range, cannot complete like this transformationreation.As given water outlet/dry gas mol ratio 0～2.0, if water/dry gas mol ratio is 0, certainly cannot there is transformationreation, because transformationreation is the reaction of water vapour and CO, there is no water vapour, with what carry out transformationreation? how about carry out transformationreation? if water/dry gas mol ratio is 2.0, too high water-gas ratio very easily causes catalyzer reversal of cure, is also to maintain shift conversion step long-period stable operation.For a set of scientific and reasonable CO shift process is set, catalyzer air speed when water/dry gas mol ratio of given each the shift converter import accurately of necessary needs and temperature out scope, conversion gas and conversion gas process conversion bed, otherwise in shift converter, serious side reaction can occur, CO changing device can not normally move certainly.
The first step shift-reaction step of 2, speaking approvingly of in invention is adiabatic transformationreation, first step transformationreation the first conversion gas temperature is out 400～500 ℃, not providing water/dry gas mol ratio and the air speed of the concrete conversion gas that enters first step transformationreation, there is serious methanation side reaction for the high concentration CO transformationreation of low water-gas ratio in this temperature range! Cannot carry out normal transformationreation at all.
3, whether isothermal shift converter adopts pump circulation to move heat, depends on the specification of isothermal shift converter according to what condition designs.In fact the specification of isothermal shift converter is to carry out calculative determination by the conversion tolerance of passing through, rather than the reaction heat intensity being shifted out by needs decides and dominates, so natural circulation that adopts density difference to promote, can meet shifting out in time of reaction heat completely, can save facility investment, reduce device operation energy consumption simultaneously.
In a word, for transformationreation flow scheme design, can only must be also to design targetedly according to concrete gasification technology, do not have at present a kind of converter technique can meet the crude synthesis gas that various kinds of coal gas technology generates simultaneously.In shift process design,, may there is absurd and a catastrophic consequence in wide in range operating temperature range and wide in range water-gas ratio parameter.Once had the water-gas ratio of certain shift conversion step first shift converter in startup procedure to be displaced to 0.25 by intrinsic 0.18, and finally caused the first shift converter outlet conversion gas temperature to rise violently 580 ℃ by 400 ℃! There is the side reactions such as serious methanation, found not only there is methane gas in outlet conversion gas by analytical test, also had ethylene gas!
Summary of the invention
The series of problems such as technical problem to be solved by this invention is to provide a kind of low water-gas ratio to become in advance string isothermal CO conversion process for the present situation of prior art, and the technical process of the low aqueous vapor high concentration CO of existing shell converter technique is long, calorific loss is many to solve, the easy overtemperature of shift converter, catalyst life are short and energy consumption is high.
The present invention solves the problems of the technologies described above adopted technical scheme: this low water-gas ratio becomes string isothermal CO conversion process in advance, it is characterized in that comprising the steps:
First the raw gas that gasification process is sent here enters gas-liquid separator separates and goes out liquid phase, enter raw gas interchanger with then and be to enter detoxification groove after middle pressure superheated vapour that 400 ℃, pressure are 4.0MPa fully mixes to remove the impurity in raw gas from the temperature of pipe network from the conversion gas mixture heat exchange to 190 of isothermal shift converter ℃～230 ℃; The raw gas temperature that control enters detoxification groove is that 200～220 ℃, water/dry gas mol ratio are 0.19～0.23;
Enter pre-shift converter by detoxification groove raw gas out and carry out preliminary transformationreation, rough coal air water/dry gas mol ratio that control enters pre-shift converter is 0.19～0.23, temperature is 200～220 ℃, controlling pre-shift converter inner catalyst air speed is 5000～7000, the pre-change mixture temperature that goes out pre-shift converter is 360 ℃～390 ℃, and CO butt volume content is about 34%～38%;
Convert 251 ℃ of self-produced temperature to middle pressure superheated vapour and isothermal that to supplement in pre-change gas mixture from the temperature of pipe network be 4.0MPa into 400 ℃, pressure, the middle pressure saturation steam of pressure 4.0MPa, regulating pre-change to mix air water/dry gas mol ratio is 0.50～0.55, enters in gas liquid mixer; Feed water to pre-change gas mixture Quench humidification to filling into 215 ℃ of medium pressure boilers in gas liquid mixer simultaneously, and pre-water/dry gas mol ratio and the temperature that becomes gas mixture of fine setting again, making the temperature of the exit gas of gas liquid mixer be down to 245 ℃～255 ℃, water/dry gas mol ratio is 0.60～0.70, then enter isothermal shift converter and carry out depth conversion, controlling isothermal shift converter inner catalyst air speed is 1000～3000, and the temperature of isothermal shift converter is 250～270 ℃.
Isothermal shift converter well-defined reaction temp is controlled at 250 ℃ of left and right, allows temperature of reaction to have the fluctuation of 10 ℃～20 ℃.
The isothermal conversion gas temperature that goes out isothermal shift converter is 260 ℃～270 ℃, and CO butt volume content is 1.0%～1.5%, and isothermal conversion gas enters after raw gas preheater adds hot raw gas and send downstream to carry out waste heat recovery;
In isothermal shift converter, the import of heat transfer tube connects the oiler feed outlet of drum, oiler feed becomes the middle pressure saturation steam of 251 ℃ of pressure 4.0MPa, temperature after absorbing heat in isothermal shift converter, in this, press saturation steam to enter after drum is isolated liquid phase and sent and all sneaked in pre-change gas mixture by drum top, the liquid phase that discharge drum bottom is entered in isothermal shift converter and is recycled by self-circulation mode; Fed water to supplementing medium pressure boiler in drum by battery limit (BL), to maintain the stable of liquid level of steam drum simultaneously.
The isothermal shift converter using in above-mentioned technique can use any one isothermal shift converter of the prior art.
Preferably, described isothermal shift converter can comprise:
Body of heater, is closure casing, and the top of body of heater is provided with reaction gas entrance and inspection manhole, and the upper portion side wall of body of heater is provided with cooling water outlet, and bottom of furnace body is provided with cooling water inlet;
Heat-exchanging tube bundle, is arranged in described body of heater, is made up of the many heat transfer tubes that are parallel to each other;
Gas distributor, is arranged in described body of heater, and the gas entering in body of heater enters beds after gas distributor current-sharing;
Upper tubesheet and lower tubesheet, be connected to the upper/lower terminal of described gas distributor, which is provided with multiple pores, and the two ends of each heat transfer tube are plugged in respectively in pore corresponding on upper and lower tube sheet;
Gas trap, for collecting reacted synthetic gas, is longitudinally arranged on described body of heater middle part;
It is characterized in that:
Described body of heater comprises the epimere, stage casing and the hypomere that are detachably connected, and the top of described body of heater is also provided with conversion gas outlet; The lower end of described gas trap connects described lower tubesheet, and described upper tubesheet is provided with connecting hole, and the upper end of described gas trap is through this connecting hole escape pipe that removably connects; The other end of this escape pipe exports and exposes to described body of heater through described conversion gas;
The top of the described upper tubesheet annular upper cover that is tightly connected, be tightly connected described body of heater between described stage casing and described hypomere of described lower tubesheet.
Preferably, above-mentioned three sections of bodies of heater can connect by flange, and body of heater can be bearing in vertical placement on skirt.
In order to facilitate the filling of catalyzer, described gas distributor can comprise the multiple segmentations that are detachably connected, and each segmentation is removably connected and formed by two semicircular cylinders again.
Further, distributing homogeneity when guaranteeing that gas enters beds, each described segmentation all can include outer cylinder body and be set in the inner barrel in described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected to form and is set in inner core in described urceolus, and described outer cylinder body and described inner barrel interval gapped.Inner barrel plays the effect of quadratic distribution to reaction gas.
Resistance to flow when reducing gas quadratic distribution, the density of the pore on described inner core can be greater than the density of described urceolus, and the aperture of pore on described inner core is less than or equal to 3mm.
Consider the settlement issues of catalyzer in production process, described gas distributor is not offered pore near described upper tubesheet 100mm with interior position, to prevent that the reaction gas that catalyst sedimentation causes from refluxing and short circuit.
In order to remove timely and effectively reaction heat, described cooling water outlet can have two, and the rising pipe that connects described upper cover and two cooling water outlets also has two.The design of two cooling water outlets can be accelerated flowing of water coolant, thereby rapid moving is except reaction heat.
Consider the thermal expansion of water pipe and the thermal expansion of gas trap, can on described rising pipe, be provided with expansion joint; Described gas trap is positioned in the part of described upper cover and described body of heater cavity and is also provided with expansion joint.
The mode of connection of upper tubesheet and body of heater can have multiple, preferably, can on the sidewall of described upper tubesheet, be interval with polylith preset pieces, accordingly, the inner side-wall of described body of heater is provided with many group strongbacks, every group of strongback comprises left and right spaced left strongback and right strongback, and each described preset pieces is between the left and right strongback of correspondence.
Described gas-collecting pipe part between upper lower tubesheet is provided with multiple pores evenly and at intervals, and described gas-collecting pipe is near not perforate in upper tubesheet bottom surface 100mm, to prevent that the catalyst sedimentation gas that induces reaction from refluxing and short circuit.
The upper surface of described lower tubesheet is provided with adapter sleeve, and it is interior and gapped with the upper surface interval of described lower tubesheet that the bottom of described gas trap is positioned at this adapter sleeve.Arranging of gap is mainly the dimensional change space for thermal expansion is provided.
Above-mentioned isothermal shift converter adopts overall diameter to Π type structure on the whole, on reaction gas is enterprising, go out, loading catalyst between heat transfer tube, in pipe, walk water coolant, water coolant absorbs conversion heat, the requirement of strength shifting out according to reaction heat, cooling water circulation process can be that natural circulation can be also pump circulation, recirculated cooling water downstream can arrange drum byproduct steam recovery waste heat.Maintain the constant of transformationreation temperature by the controlled circulation water yield.
Conversion process provided by the present invention adopts the CO conversion process of adiabatic reactor to compare with existing whole process, and the present invention has following feature:
1, shift process is short, and resistance is little, and after saving, the compression work of system, has reduced energy consumption.
2, use isothermal shift converter to substitute at least adiabatic shift converter of two-stage, reduced shift converter number of units, saved facility investment.
3, the operation of isothermal shift converter is gentle, there will not be overtemperatute, can effectively guarantee the work-ing life of catalyzer, and shift conversion step operation is more stable;
4, the self-produced steam of shift conversion step, all for the transformationreation of self, has saved part sect heat-exchanger and energy recovery equipment, has simplified technical process, has saved facility investment.
Compare with existing shunting-type isothermal sulfur-tolerant conversion process, the present invention has following advantage:
1, before pre-shift converter, be provided with detoxification equipment, the crude synthesis gas of sending here from gasification filtered, better protecting transformation catalyst, extended work-ing life of catalyzer, reduced the process cost of shift conversion step, shift conversion step operation is simultaneously more stable;
2, pre-shift converter inner catalyst adopts high-speed operation, and in stove, temperature is no more than 400 ℃, and pre-change catalyzer long service life, methanation side reaction can not occur at this temperature, can guarantee that transformationreation steadily carries out.
3, the specification based on isothermal shift converter is to be determined by the conversion tolerance of passing through, rather than the reaction heat intensity being shifted out by needs decides and dominates, so natural circulation that adopts density difference to promote, can meet shifting out in time of reaction heat completely, cancel the pump for pump circulation, save facility investment, reduced device operation energy consumption.
4, by the reasonably optimizing to shift process, shift conversion step institute producing steam, all for self transformationreation, has been cancelled vapor superheater, has reduced facility investment.
Isothermal shift converter in preferred version of the present invention is compared with isothermal shift converter of the prior art, and cooling water circulation resistance is little, can high-speed circulating, shift out fast high concentration CO reaction heat thereby reach; The object that therefore can reach by the controlled circulation water yield control change temperature of reaction, cooling water outlet can arrange drum byproduct steam, recovery waste heat, structure of reactor is simple, less investment, controllability is strong.Cooling water outlet pipe, gas trap and body of heater all adopt flange to be connected, making outside body of heater is detachably epimere, stage casing and hypomere three parts, internal-response system can entirety be extracted out, add that the sectionally smooth join design of gas distributor and quick handling that removable bolt structure is catalyzer and the checking maintenance of post facility provide convenience.Take into full account high temperature stress operating mode, be provided with expansion joint in two the gentle body collector of circulating cooling water out upper ends of internal-response system, solved the thermal expansion upwards of internal-response entire system; At the bottom of gas-collecting pipe, location, sleeve gap, has solved the downward differential expansion of gas-collecting pipe, and this is conducive to the long-period stable operation of equipment and the prolongation in work-ing life.CO overall diameter adopts full radial structure to isothermal shift converter, and circulation area is large, and bed resistance is little, and pressure drop is little.Gas distributor adopts inside and outside barrel structure, to reaction gas quadratic distribution, make gas distribution more even, be conducive to improve transformation efficiency, simultaneously, take into full account catalyst sedimentation problem, be all reserved with not aperture area of 100mm at gas distributor top and gas-collecting pipe near upper tubesheet place, can prevent that the conversion gas that catalyst sedimentation causes from refluxing, short circuit.The overall diameter that shift converter adopts is to Π type structure, on reaction gas is enterprising, go out, taking full advantage of radial reactor flow manifold static pressure raises along fluid flow direction, the feature that afflux runner static pressure streamwise reduces, be conducive to conversion gas being uniformly distributed and steady flow at beds, make reaction more stable, conversion efficiency is high.The present invention adopts shell and tube-type reactor, between catalyst loading heat transfer tube, and reaction bed temperature, stable, the life-span is long, can increase CO conversion gas treatment capacity by increasing gas distributor hop count mode, is conducive to the maximization of device; And utilize the feature that radial reactor resistance is little can improve air speed, increase transformation efficiency, improve the throughput of equipment.
Accompanying drawing explanation
Fig. 1 is the cross-sectional schematic of the embodiment of the present invention 1 assembly structure;
Fig. 2 is the enlarged view of position 532 in Fig. 1 of the present invention;
Fig. 3 is the floor map of locating structure between upper tubesheet and inboard wall of furnace body in the embodiment of the present invention 1;
Fig. 4 is gas distributor structural representation in the embodiment of the present invention 1;
Fig. 5 be along A-A in Fig. 4 to sectional view;
Fig. 6 is the floor map of annular seal head in the embodiment of the present invention 1;
Fig. 7 is the process flow diagram of the embodiment of the present 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 tons/year of urea of 300,000 tons/year of synthetic ammonia, the present invention being described in further detail.
The structrual description of the isothermal shift converter 5 using in the present embodiment as shown in Figures 1 to 6, is as follows:
As shown in Figures 1 to 6, this CO overall diameter comprises to isothermal shift converter:
Body of heater 51, comprises epimere 515, stage casing 512 and hypomere 511, and epimere 515 is for being welded with the ellipsoidal head of straight section, between epimere 515 and stage casing 512, all adopt flange to removably connect between stage casing 512 and hypomere 511.The end socket top of epimere 515 is provided with reaction gas entrance 516, conversion gas outlet 517 and top inspection manhole 518, its straight section sidewall is provided with two the circulating cooling water out 514A and the 514B that are arranged symmetrically with, hypomere 511 bottoms are provided with cooling water inlet 519, body of heater 1 bottom is seated on skirt 55, and skirt 55 is the base for supporting of this isothermal shift converter.
In body of heater, by the heat-exchanging tube bundle being made up of many heat transfer tubes 537, the middle part of heat-exchanging tube bundle is provided with multiple for supporting the strut member 536 of heat-exchanging tube bundle.The two ends of each heat transfer tube are plugged in respectively in pore corresponding on upper tubesheet 534 and lower tubesheet 531 and form heat-exchanging tube bundle, in the gap between each heat transfer tube, are filled with catalyzer.
Heat-exchanging tube bundle outside is wrapped up by the gas distributor 54 of tubular, gas distributor 54 is connected to form by the gas distributor pipe nipple bolt of several sections of same structures, every section of sparger includes inner barrel 545 and the outer cylinder body 544 that length is 500mm, and inside and outside cylindrical shell forms by two semicircular cylinders, semicircular cylinder end is welded with two groups of vertical web plates 543, and two semicircular cylindrical shell bolts are formed to columniform cylindrical shell together; After each section of inner barrel connects, form inner core, after each section of outer cylinder body connects, form sheathed urceolus outer tube.On inner barrel 545 and outer cylinder body 544, be evenly equipped with respectively circular pore as reactant gas passage, inner core is as gas quadratic distribution device, its perforate density is greater than urceolus and aperture is not more than 3mm, the top of inner core and urceolus and bottom are equipped with two and half ring flat-plates 541, half ring flat-plate split position is consistent with inner core and urceolus, and weld together with vertical web plate 543, half ring flat-plate 541 ends are provided with eight journal stirrups 542, for bolt and location between upper-lower section gas distributor, the upper end of epimere sparger relies on the retaining ring 5311 welding with upper tubesheet 534 to locate, the ring groove location that lower tubesheet 531 is opened is put in the lower end of hypomere cylindrical shell, simultaneously, in the one section of gas distributor in the top, urceolus is apart from not offering pore within upper tubesheet 100mm height location, to prevent the catalyst sedimentation road of breathing hard that induces reaction.The segmentation bolt releasable connection design of gas distributor, can effectively improve the handling of catalyzer and change efficiency.
As shown in Figure 7, to become in advance string isothermal CO conversion process step as follows for the low water-gas ratio of the present embodiment:
160 ℃ of the raw gas temperature of the saturated water vapour of 1. being sent here by Shell Coal Gasification workshop section, pressure 3.7MPa, with pipeline by raw gas from gasification workshop section delivers to the process of conversion section due to calorific loss, a small amount of water vapour in raw gas generation phlegma that can be condensed, raw gas and lime set coexist and can cause corrosion and the vibrations of pipeline and equipment in tubing system, so raw gas needed lime set wherein to separate before entering pre-shift converter, therefore the present embodiment is first sent into raw gas gas-liquid separator 1, liquid flows out from the outlet at bottom of gas-liquid separator 1.By the gas-liquid separator 1 top raw gas after separatory out through raw gas preheater 6 and isothermal conversion gas heat exchange temperature raising to 190 ℃～230 ℃, again with from 400 ℃ of pipe network temperature, the a small amount of middle superheated vapour of pressing of pressure 4.0MPa fully mixes, regulating water/dry gas mol ratio is 0.19～0.23, enters detoxification groove 2 and removes the impurity such as ash content and heavy metal in raw gas.
Rough coal air water/dry gas mol ratio that control enters detoxification groove 2 is 0.18～0.22, then enters pre-shift converter 3 and carries out preliminary transformationreation, controls pre-shift converter inner catalyst air speed and be 5000～7000, water/dry gas mol ratio is 0.18～0.22, the pre-change mixture temperature that goes out pre-shift converter 3 is 360 ℃～390 ℃, and CO butt volume content is about 34%～38%, to supplementing in pre-change gas mixture from 400 ℃ of the temperature of pipe network, middle pressure superheated vapour and the isothermal of pressure 4.0MPa convert 251 ℃ of self-produced temperature, the middle pressure saturation steam of pressure 4.0MPa, regulating pre-change to mix air water/dry gas mol ratio is 0.50～0.55, then enter in gas liquid mixer 4, with 215 ℃ of medium pressure boiler feedwater, pre-change gas mixture Quench humidification is also finely tuned to pre-change again and mix air water/dry gas mol ratio, make its temperature be down to 245 ℃～255 ℃, water/dry gas mol ratio is 0.60～0.70, enter isothermal shift converter 5 and carry out depth conversion, controlling isothermal shift converter inner catalyst air speed is 1000～3000, the temperature of isothermal shift converter is 250 ℃, 10 ℃～20 ℃ of isothermal shift converter temperature rises, the isothermal conversion gas temperature that goes out isothermal shift converter 5 is about 260 ℃～270 ℃, CO butt volume content is about 1.0%～1.5%, isothermal conversion gas enters after raw gas preheater 6 adds hot raw gas and send downstream to carry out waste heat recovery.
comparative example
Contrast in table 1 for the shunting-type isothermal sulfur-tolerant conversion process and the adiabatic conversion process significant parameter of isothermal conversion string that are matched in the gas making of identical scale Shell Coal Gasification.
Table 1
Claims (10)
1. low water-gas ratio becomes a string isothermal CO conversion process in advance, it is characterized in that comprising the steps:
First the raw gas that gasification process is sent here enters gas-liquid separator separates and goes out liquid phase, enter raw gas interchanger with then and be to enter detoxification groove after middle pressure superheated vapour that 400 ℃, pressure are 4.0MPa fully mixes to remove the impurity in raw gas from the temperature of pipe network from the conversion gas mixture heat exchange to 190 of isothermal shift converter ℃～230 ℃; The raw gas temperature that control enters detoxification groove is that 200～220 ℃, water/dry gas mol ratio are 0.19～0.23;
Enter pre-shift converter by detoxification groove raw gas out and carry out preliminary transformationreation, rough coal air water/dry gas mol ratio that control enters pre-shift converter is 0.19～0.23, temperature is 200～220 ℃, controlling pre-shift converter inner catalyst air speed is 5000～7000, the pre-change mixture temperature that goes out pre-shift converter is 360 ℃～390 ℃, and CO butt volume content is 34%～38%;
Convert 251 ℃ of self-produced temperature to middle pressure superheated vapour and isothermal that to supplement in pre-change gas mixture from the temperature of pipe network be 4.0MPa into 400 ℃, pressure, the middle pressure saturation steam of pressure 4.0MPa, regulating pre-change to mix air water/dry gas mol ratio is 0.50～0.55, enters in gas liquid mixer; Feed water to pre-change gas mixture Quench humidification to filling into 215 ℃ of medium pressure boilers in gas liquid mixer simultaneously, and pre-water/dry gas mol ratio and the temperature that becomes gas mixture of fine setting again, making the temperature of the exit gas of gas liquid mixer be down to 245 ℃～255 ℃, water/dry gas mol ratio is 0.60～0.70, then enter isothermal shift converter and carry out depth conversion, controlling isothermal shift converter inner catalyst air speed is 1000～3000, and the temperature of isothermal shift converter is 250～270 ℃;
The isothermal conversion gas temperature that goes out isothermal shift converter is 260 ℃～270 ℃, and CO butt volume content is 1.0%～1.5%, and isothermal conversion gas enters after raw gas preheater adds hot raw gas and send downstream to carry out waste heat recovery;
In isothermal shift converter, the import of heat transfer tube connects the oiler feed outlet of drum, oiler feed becomes the middle pressure saturation steam of 251 ℃ of pressure 4.0MPa, temperature after absorbing heat in isothermal shift converter, in this, press saturation steam to enter after drum is isolated liquid phase and sent and all sneaked in pre-change gas mixture by drum top, the liquid phase that discharge drum bottom is entered in isothermal shift converter and is recycled by self-circulation mode; Fed water to supplementing medium pressure boiler in drum by battery limit (BL), to maintain the stable of liquid level of steam drum simultaneously.
2. low water-gas ratio according to claim 1 becomes string isothermal CO conversion process in advance, it is characterized in that described isothermal shift converter comprises:
Body of heater, is closure casing, and the top of body of heater is provided with reaction gas entrance and inspection manhole, and the upper portion side wall of body of heater is provided with cooling water outlet, and bottom of furnace body is provided with cooling water inlet;
Heat-exchanging tube bundle, is arranged in described body of heater, is made up of the many heat transfer tubes that are parallel to each other;
Gas distributor, is arranged in described body of heater, and the gas entering in body of heater enters beds after gas distributor current-sharing;
Upper tubesheet and lower tubesheet, be connected to the upper/lower terminal of described gas distributor, which is provided with multiple pores, and the two ends of each heat transfer tube are plugged in respectively in pore corresponding on upper and lower tube sheet;
Gas trap, for collecting reacted synthetic gas, is longitudinally arranged on described body of heater middle part;
Described body of heater comprises the epimere, stage casing and the hypomere that are detachably connected, and the top of described body of heater is also provided with conversion gas outlet; The lower end of described gas trap connects described lower tubesheet, and described upper tubesheet is provided with connecting hole, and the upper end of described gas trap is through this connecting hole escape pipe that removably connects; The other end of this escape pipe exports and exposes to described body of heater through described conversion gas;
The top of the described upper tubesheet annular upper cover that is tightly connected, be tightly connected described body of heater between described stage casing and described hypomere of described lower tubesheet.
3. low water-gas ratio according to claim 2 becomes string isothermal CO conversion process in advance, it is characterized in that described gas distributor comprises the multiple segmentations that are detachably connected, and each segmentation has again two semicircular cylinders formation that removably connects.
4. low water-gas ratio according to claim 3 becomes string isothermal CO conversion process in advance, it is characterized in that each described segmentation includes outer cylinder body and is set in the inner barrel in described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected to form and is set in inner core in described urceolus, and described outer cylinder body and described inner barrel interval gapped.
5. low water-gas ratio according to claim 4 becomes string isothermal CO conversion process in advance, and the density that it is characterized in that the pore on described inner core is greater than described urceolus, and the aperture of pore on described endoporus is more than or equal to 3mm.
6. low water-gas ratio according to claim 5 becomes string isothermal CO conversion process in advance, it is characterized in that described gas distributor do not offer pore near described upper tubesheet 100mm with interior position.
7. become in advance string isothermal CO conversion process according to the low water-gas ratio described in the arbitrary claim of claim 2 to 6, it is characterized in that described cooling water outlet has two, the rising pipe that connects described upper cover and two cooling water outlets also has two.
8. low water-gas ratio according to claim 6 becomes string isothermal CO conversion process in advance, it is characterized in that described rising pipe is provided with expansion joint; Described gas trap is positioned in the part of described upper cover and described body of heater cavity and is also provided with expansion joint.
9. low water-gas ratio according to claim 7 becomes string isothermal CO conversion process in advance, it is characterized in that being interval with polylith preset pieces on the sidewall of described upper tubesheet, accordingly, the inner side-wall of described body of heater is provided with many group strongbacks, every group of strongback comprises left and right spaced left strongback and right strongback, and each described preset pieces is between the left and right strongback of correspondence.
10. low water-gas ratio according to claim 8 becomes string isothermal CO conversion process in advance, it is characterized in that the not perforate in close upper tubesheet bottom surface 100mm of described gas trap; The upper surface of described lower tubesheet is provided with adapter sleeve, and it is interior and gapped with the upper surface interval of described lower tubesheet that the bottom of described gas trap is positioned at this adapter sleeve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210378068.4A CN102887481B (en) | 2012-10-08 | 2012-10-08 | Low water-gas ratio pre-conversion constant-temperature CO conversion technology |
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| CN103435006B (en) * | 2013-08-20 | 2015-04-08 | 湖南安淳高新技术有限公司 | High-CO high-conversion-rate isothermal shift reactor |
| CN103881768B (en) * | 2014-03-24 | 2015-05-27 | 中石化宁波工程有限公司 | Cyclic CO (carbon monoxide) transformation process |
| CN104150439B (en) * | 2014-07-21 | 2016-06-15 | 中国五环工程有限公司 | Carbon monoxide transformation technical |
| CN104152187B (en) * | 2014-08-06 | 2016-02-17 | 中石化宁波工程有限公司 | A kind of can the CO conversion process in extending catalyst work-ing life |
| CN106115700B (en) * | 2016-08-19 | 2018-02-13 | 南京聚拓化工科技有限公司 | Beam tube type water bed moves the compound CO converting means of heat and conversion process |
| CN109181782B (en) * | 2018-09-30 | 2020-07-24 | 中石化宁波工程有限公司 | Air-cooling and water-cooling isothermal transformation process matched with coal water slurry gasification |
| CN109534288A (en) * | 2018-12-12 | 2019-03-29 | 安徽金禾实业股份有限公司 | A kind of synthesis ammonia isothermal converting means and method |
| 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 |
| CN113501492B (en) * | 2021-07-06 | 2022-09-06 | 中石化宁波工程有限公司 | Long-period transformation process for adjusting water-gas ratio by two-step method for oxo synthesis |
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| CN102250658A (en) * | 2010-05-19 | 2011-11-23 | 上海标氢气体技术有限公司 | Method for preparing liquefied natural gas by converting raw materials of coke oven gas and blast furnace gas |
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