CN201058854Y - Fixed bed device for F-T synthesis - Google Patents
Fixed bed device for F-T synthesis Download PDFInfo
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- CN201058854Y CN201058854Y CNU2007201495897U CN200720149589U CN201058854Y CN 201058854 Y CN201058854 Y CN 201058854Y CN U2007201495897 U CNU2007201495897 U CN U2007201495897U CN 200720149589 U CN200720149589 U CN 200720149589U CN 201058854 Y CN201058854 Y CN 201058854Y
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Abstract
The utility model provides a fixed bed device for Fischer-Tropsch synthesis to prepare liquid hydrocarbon, comprising a heater, a reactor connected with the upper part of the heater and a casing pipe which is sleeved outside the reactor and connected with the heater, wherein, a heating medium flue gas pipeline is arranged inside the heater; an inlet of the flue gas pipeline is arranged on the upper part of the heater; an outlet of the flue gas pipeline is arranged on the lower part of the heater; circulating water entering into the heater is heated through the flue gas pipeline; an inlet and an outlet for the circulating water are respectively arranged on the wall of the heater; the outlet for the circulating water is arranged on the upper part of the heater and communicated with the casing pipe outside the reactor; a feed gas pipeline is arranged inside the heater; a feed gas inlet and a feed gas outlet are arranged on the wall of the heater; the feed gas outlet is communicated with the reactor. The fixed bed device for Fischer-Tropsch synthesis can effectively solve the problem that the Fischer-Tropsch synthesis is too high in reaction heat, ensures the sufficient reaction of feed gas, and improves the conversion rate of the Fischer-Tropsch synthesis reaction.
Description
Technical field
The utility model provides a kind of fixed bed device, and it is the device that is used for Fischer-Tropsch synthesis, refer in particular to utilize a kind of through fixed bed device improvement, synthetic gas can more fully be changed into liquefied hydrocarbon by Fischer-Tropsch synthesis.
Background technology
Since the worsening shortages of petroleum resources and poor qualityization, along with the continuous increase of processed oil demand, and the increasingly stringent of environmental regulation, obtain the liquid processed oil fuel of fine by new method, be the significant problem that the current China and even the whole world face.Fischer-Tropsch is synthetic to be to utilize H
2With CO be the process of main component synthetic hydrocarbon under the effect of catalyzer, be the new way of producing liquid fuel, also be the most promising the most effective technology at present.It can be used for coal system oil, the multiple course of processing of Sweet natural gas system wet goods.
According to the difference of catalyzer, the Fischer-Tropsch synthesis device can have various ways, for example fixed bed, gas-solid fluidized bed and slurry attitude bed etc.Wherein gas-solid fluidized bed complicated operation, easy carbon distribution, less now use.Slurry attitude bed accessory has heat-transfer effect good, and temperature of reaction is easy to advantages such as control, is the main flow of Fischer-Tropsch synthesis device development.But the per pass conversion of paste state bed reactor is low, and the solid-liquid separation difficulty only is suitable for large-scale synthetic oil device.Fixed bed then has simple to operate, and the flexile characteristics of form have very big magnetism for numerous middle-size and small-size synthetic oil devices, but the fixed-bed heat transfer performance bad be the restriction its development important factor.
Traditional used for Fischer-Tropsch synthesis fixed bed device is to take gas feeding manner from top to bottom, heat transferring medium from top to bottom circulated in countercurrent in sleeve pipe.A large amount of reaction heat that this heat exchange mode can not be discharged the beds front end effectively shift out rapidly, cause reactor " temperature runaway " easily, make to generate the decline of purpose product selectivity, and are easy to form carbon distribution.And adopt the gas per pass conversion of fixed bed device not high, and need utilize power set to carry out the tail gas circulation, increased the running cost of device.
The utility model content
The utility model provides a kind of novel fixed bed device that is used for Fischer-Tropsch synthesis, this device can make reaction heat effectively shift out, avoid occurring reaction focus and temperature runaway phenomenon, make the whole reaction system temperature maintenance in " constant temperature scope ", guaranteed that successful reaction carries out, and, improved the per pass conversion of synthetic gas dramatically by carrying out many bank of reactor operations, tail gas need not be circulated.
The purpose of this utility model is to provide a kind of fixed bed device that is used for Fischer-Tropsch synthesis, by this novel fixed bed device, make synthetic gas (unstripped gas) enter the beds generation Fischer-Tropsch synthesis of reactor from the fixed bed bottom, feed recirculated water in the sleeve pipe outside reactor, recirculated water absorbs heat at reactor lower part, the top heat release, thereby keep the homo(io)thermism of reactor, promptly guaranteed the homo(io)thermism of catalyst reactor layer reaction, stopped the generation of temperature runaway, method of the present utility model is particularly useful for the production process of the liquid hydrocarbon simply and easily of middle-size and small-size scale.
The purpose of this utility model can be achieved through the following technical solutions.
The utility model provides a kind of fixed bed device that is used for Fischer-Tropsch synthesis, it is characterized in that: it is made up of this fixed bed device the fixed bed that two groups of head and the tail are contacted mutually at least, every group of fixed bed includes reactor, the corresponding well heater that is connected with this reactor, the sleeve pipe that joins with this well heater, interchanger (also can be described as condenser) and triphase separator, wherein, be provided with unstripped gas pipeline and heating medium pipeline in the well heater of every group of fixed bed, the wall of well heater is provided with unstripped gas inlet and unstripped gas outlet, this unstripped gas outlet is connected with this bank of reactor, also be provided with the heating medium inlet on the well heater wall, the heating medium outlet, and the recirculated water of well heater inlet and circulating water outlet, the circulating water outlet of every group of well heater communicates with this group sleeve pipe, all is connected with interchanger and triphase separator successively between the reactor of described two groups of polyphones.
The inside of above-mentioned reactor also is equiped with catalyzer, so the inside of this reactor also can be described as beds.
Thereby the utility model enters beds generation Fischer-Tropsch synthesis by making unstripped gas from the bottom of reactor, and (space between reactor outer wall and the internal surface of sleeve pipe) feeds recirculated water in the sleeve pipe outside reactor, the traffic direction of recirculated water in sleeve pipe is identical with the traffic direction (from bottom to top) of unstripped gas in reactor, promptly, recirculated water absorbs heat at reactor lower part, the top heat release, thereby keep the homo(io)thermism of reactor, stop the generation of temperature runaway, improved the per pass conversion of synthetic gas.
Said fixing bed apparatus of the present utility model, fixed bed by two groups or more is contacted from beginning to end, wherein every group of fixed bed includes the reactor that is used to take place Fischer-Tropsch synthesis, the well heater that is used for heating cycle water and reactant gases (unstripped gas), the sleeve pipe that is used for the recirculated water fluid interchange, wherein all be connected between every group of sleeve bottom and this group well heater and communicate, and respectively organize and all be interconnected up and down between the sleeve pipe with the holding temperature pressure equilibrium, when making unstripped gas pass through reactor, can under the effect of catalyzer, react, two or more sets reactors are contacted mutually, can so that in first bank of reactor unreacted completely unstripped gas continue to enter in next bank of reactor and proceed building-up reactions, reach the purpose of abundant reaction.
In the above-mentioned fixed bed device of the utility model, the bottom of described each bank of reactor preferably also is connected with product collector and product groove successively, this product collector is to be used for being collected in reacting the liquid product that the boiling point that generates is higher than temperature of reaction in this reactor, this product groove is to be used for collecting the product that transports out from this product collector, and this product preferably passes through the product of reduced pressure treatment.
In preferred implementation of the present utility model, the top of described each bank of reactor all is connected with the interchanger (condenser) of tool condensation successively, the triphase separator of tool centrifugation, the product that reaction is generated is flowed through behind this interchanger and the triphase separator, elder generation's condensation, to sift out liquid hydrocarbon product (be used for by this interchanger that reaction generates in this reactor of condensation and from the effusive boiling point of this reactor top lower hydro carbons and water) and unconverted synthetic gas, in this triphase separator, the lower hydro carbons of above-mentioned boiling point and water and unconverted synthetic gas are carried out water again, oil phase and gas phase separation, oil phase can be sent in the described product groove as the cryogenic condensation product after reducing pressure, the water decompression rectifiable recovery in back, gas phase then enters next bank of reactor and continues reaction, so that the reaction of unstripped gas is more abundant.Last bank of reactor tail gas is separated the direct emptying in back or burning utilizes its energy, no longer continues reaction.
For the recirculated water that circulates in the well heater is heated, the well heater of fixed bed device of the present invention can adopt any known type of heating, in preferred embodiment of the present utility model, what the heating medium of well heater adopted is stack gas, promptly, the said fixing bed apparatus is preferably flue gas duct at the heating medium pipeline that the inside of well heater is provided with, the heating medium inlet that the wall of well heater is provided with is preferably the waste gas inlet, the heating medium outlet is preferably flue gas outlet, this waste gas inlet is preferably on the top of well heater, flue gas outlet is used for making the recirculated water of well heater internal operation to be heated to preset temperature in the bottom.
In order to realize the circulation of recirculated water in the fixed bed device of the present utility model, recirculated water moves in sleeve pipe and flows out, this telescopic circulating water outlet place also is connected with (or extension is connected with) water tank, be used for storing effusive recirculated water from this sleeve pipe, this water tank can be regulated temperature, pressure and the liquid level of described recirculated water timely.Preferably also be provided with liquidometer and/or turnover valve on this water tank, and more preferably also be provided with explosion trap, cause the too fast potential safety hazard of hydraulic pressure rising owing to heat absorption is excessive in order to the situation of level monitoring and elimination in time.
In fixed bed device of the present utility model, described water tank lower end is provided with the circulation line that the recirculated water inlet offered on the wall with well heater communicates, when rising to the water tank at sleeve pipe top because of recirculated water, temperature descended after itself and the external world carried out heat exchange, then, begin circulation from the circulation line of outside because the effect of gravity or recycle pump flows down to reenter sleeve bottom.This circulation line can be divided into self-heating circulation line and/or high-pressure pump pump circulation, and high-pressure pump circulation line i.e. pipeline is provided with high-pressure circulation pump, so that realize circulation under the highly compressed state.
In preferred embodiment of the present utility model, unstripped gas pipeline and the heating medium pipeline established in the well heater are preferably spiral pipe, purpose is in order to increase the area of heat transfer heat exchange, and heating medium pipeline (flue gas duct) is the up pipeline of spirrillum more preferably.
The utility model utilizes the said fixing bed apparatus to carry out Fischer-Tropsch synthetic method and may further comprise the steps:
H
2With CO be main component (H
2/ CO is than for 0.5-5.0) fresh synthesis gas (unstripped gas) enter in the well heater that described fixed bed device bottom is provided with, in the unstripped gas pipeline, flow, after the recirculated water of quilt heat is heated to suitable preheating temperature, this synthetic gas enter with from bottom to up feeding manner and the beds by this fixed bed device so that Fischer-Tropsch synthesis to take place, and with being arranged on this fixed bed device in the outer sleeve pipe from bottom to up the recirculated water of operation carry out the indirect heat exchange, be 180-350 ℃ preferably in temperature of reaction, pressure is that 1.0-5.0MPa and pilot wire speed are to react under the 0.02-3.2m/s condition; In the method, the preset heating temperature of recirculated water is preferably hanged down 10-20 ℃ than the temperature of reaction of Fischer-Tropsch synthesis.
In order to reach the purpose of this utility model and effect, in preferred embodiment of the present utility model, above-mentioned fixed bed device is in series by two groups of fixed beds (from beginning to end) at least; The bottom of the reactor of every group of fixed bed also is provided with product collector and product groove, the top of reactor is connected with interchanger (condensation), triphase separator, the boiling point that reaction generates in this reactor is higher than the liquid product of temperature of reaction, it will flow to this product collector by self gravitation, deliver to the product groove after decompression; And lower hydro carbons and the water of boiling point that generates, it is gaseous state under temperature of reaction, will be with the top outflow reactor of unconverted synthetic gas from reactor, through after the described interchanger condensation, be sent in the described triphase separator, purpose is that water, oil phase and gas phase are separated, and wherein oil phase is delivered to the product groove as the cryogenic condensation product after reducing pressure, water decompression back rectifying is reclaimed, and gas phase then enters next bank of reactor and continues reaction.
All be connected with this in every bank of reactor bottom and organize corresponding well heater, can heat recirculated water, make recirculated water rise in the sleeve pipe with reactor in up synthetic gas carry out heat exchange; Top at this sleeve structure also is connected with water tank, can regulate temperature, pressure and the liquid level of described recirculated water timely by water tank; Be equiped with catalyzer (this catalyst layer also can be described as beds) in the inside of this reactor, described catalyzer can be cobalt-based, iron-based or other fischer-tropsch synthetic catalysts, and employed catalyzer should be able to satisfy in the cycle of long-term operation continuously active and selectivity and stablize and not breakable requirement.The outside also can preferably be provided with insulation or heating unit, plays thermoregulator effect.
For this area, the strong exothermal reaction that in fixed-bed reactor, carries out, when initial condition meets or exceeds a certain limit, the heat that the heat that reaction produces can be drained considerably beyond this system, heat a large amount of accumulation of moment occur, hot unbalance deterioration causes the reactive system temperature to present the increase of great-jump-forward, cause total system out of hand, this phenomenon is called temperature runaway.Temperature runaway all has detrimentally affect to transformation efficiency, selectivity, activity of such catalysts and the life-span etc. of reaction.
For the transformation efficiency and the selectivity that have improved fischer-tropsch reaction, fixed bed device of the present utility model preferably is in series by two bank of reactor at least.
In the technical solution of the utility model, material synthesis gas (unstripped gas) is bigger in the concentration of beds ingress, reacts more violent under catalyst action, emits a large amount of heat, bed temperature rises very fast, is reaching maximum value from inlet 1-2m place bed temperature.Comparatively high temps reaction is down accelerated, and the thermal discharge of unit time also increases, and at this moment, as can not in time removing reaction heat, the danger that causes bed " temperature runaway " is arranged.In the reactor that the utility model utilizes, recirculated water is housed in the sleeve pipe to be heated to than low 10-20 ℃ of temperature of reaction with the water temperature of high-temperature flue gas with this recirculated water in the well heater of bottom of device, reactor jacket is passed through in recirculated water and gas following current then from bottom to top, just contacted near the position that begins to react rising to unstripped gas with catalyzer, beginning is carried out heat exchange with reactor, take a large amount of reaction heat out of beds, guarantee that beds maintains the synthetic temperature of reaction.Circulating water temperature after the heat absorption raises and the part vaporization.Because along with the decline of material synthesis gas concentration, the thermal discharge of reaction tails off gradually so that on the top of beds because the thermolysis of reactor, the temperature of beds is lower than optimal reaction temperature, thereby is unfavorable for the continuation reaction of synthetic gas; The recirculated water of the comparatively high temps in the circulation tube then conducts heat to beds at this moment, guarantee that the unconverted synthetic gas of residue continues to react, recirculated water then rises in the water tank of sleeve pipe top (vapour-liquid), carry out with the external world that temperature descends after the heat exchange, then, begin new circulation because the effect of gravity flows down (perhaps under the effect of high-pressure pump) to reenter sleeve bottom from the outer loop pipeline.
In the whole process of fischer-tropsch reaction of the present utility model, the reaction bed temperature of reactor maintains " constant temperature scope " all the time, has guaranteed that successful reaction carries out, and has improved the transformation efficiency of synthetic gas, and the synthetic gas per pass conversion is reached more than 80%.And recirculated water can be taken away reaction heat and effectively cold zone be replenished rapidly because the effect of gravity is mobile very fast, and the temperature difference of water is no more than 4 ℃ up and down, has guaranteed carrying out smoothly of heat exchange, has improved the efficient of whole reactor.
The gas that the utility model comes out from last bank of reactor top comprises the light hydrocarbon product of unreacted unstripped gas and generation, and its temperature is still very high, approaches room temperature through temperature after interchanger (condensation) condensation, enters triphase separator.Wherein few lower carbon number hydrocarbons (CH
4Deng) and the unreacted unstripped gas of sub-fraction through tail gas valve emptying or as heating fuel.The liquid phase that separator comes out comprises water two portions of liquefied hydrocarbon and generation, and wherein liquid hydrocarbon enters the product collector, sends into product groove unit after the decompression and carries out deep processing, and water is sent to rectifying with the oxygen-bearing organic matter in the recycle-water.The boiling point that generates in the reaction then because the effect of self gravitation enters the product collector, send product groove unit to carry out thereafter deep processing than the high heavy hydrocarbons of temperature of reaction after decompression.
The utility model is because be provided with recirculated water in the sleeve pipe of reactor, in the well heater of bottom of device, water can be heated to temperature than low 10-20 ℃ of temperature of reaction, recirculated water and unstripped gas (synthetic gas) following current then is from bottom to top respectively by reactor jacket and beds, the huge heat that utilizes the low slightly recirculated water absorption reaction of temperature to emit in the stage of reaction beginning, hot(test)-spot temperature reduces, make it that " temperature runaway " phenomenon not take place, circulating water temperature raises, the part vaporization.Along with the gas concentration of carrying out of reacting reduces, exothermic heat of reaction reduces, temperature descends, on reactor top, pyritous recirculated water carries out heat supplement again to reactor bed, makes unreacted synthetic gas continue reaction, recirculated water then rises in the water tank at sleeve pipe top, carry out with the external world that temperature descends after the heat exchange, then, begin circulation from exterior tubing because the effect of gravity or high-pressure circulation pump flows down to reenter sleeve bottom.Whole reactor up and down temperature all is controlled at " constant temperature scope ", has guaranteed that successful reaction carries out, and has improved transformation efficiency.
The advantage that two groups of polyphone fixed beds are set is: the operative liquid hydro carbons that generates in first bank of reactor reaction comes out from reactor head with gas, enters in the interchanger condensation and removes liquid hydrocarbon product; Second bank of reactor that enters isolated gas is continuing and the reaction of first bank of reactor under same condition, and then liquid hydrocarbon product is removed in condensation once more, and unstripped gas is fully reacted, tail gas emptying.When reactor is many bank of reactor when being in series, tail gas also can enter in second group of later reactor again, and for example the 3rd bank of reactor reaches higher desirable level until the synthetic gas transformation efficiency.
The utility model can reach whole reactor up and down temperature all be controlled at the effect of " constant temperature scope ", guaranteed carrying out smoothly of fischer-tropsch reaction, and improved transformation efficiency.
Description of drawings
Fig. 1: Fischer-Tropsch of the present utility model synthesizes the single tube reactor structure iron.
Fig. 2: the fixed bed device that the Fischer-Tropsch synthesis that two groups of single tube reactors of the present utility model are formed is used.
Fig. 3: the Fischer-Tropsch synthesis fixed bed device that two groups of multitubular reactors of the present utility model are formed.
Drawing reference numeral:
1--well heater 2--high-pressure circulation pump 3--beds
4--reactor 5--sleeve pipe 6--casing wall
7--water tank 8--liquidometer 9--passes in and out valve
10--explosion trap 11--recirculated water control valve
The unstripped gas entrance of 12--well heater (or claiming well heater unstripped gas inlet)
The unstripped gas pipe outlet of 13--well heater (or claiming the outlet of well heater unstripped gas)
14--reactor gas unstripped gas is gone into the outlet of 15--reactor tail gas
16--recirculated water is gone into the inlet of 17--circulating water outlet 18--flue gas duct
The outlet 20--gas distribution grid 21--products export of 19--flue gas duct
22,25--product collector 23--interchanger (condenser) 24--triphase separator
26--water collector 27--product groove 28--tail gas blow-off valve
Embodiment
Describe the utility model in detail below in conjunction with accompanying drawing, but do not limit practical range of the present utility model.
The Fischer-Tropsch synthesis that the utility model provides is made the fixed bed device that high-quality liquid hydrocarbon is used, set reactor can be two bank of reactor in this device, also can be many bank of reactor of polyphone, wherein each reactor can be the single tube fixed bed, also can be the multitube fixed bed.
Embodiment one:
As depicted in figs. 1 and 2, present embodiment is the fixed bed device that the Fischer-Tropsch synthesis of two groups of single tube fixed-bed reactor (Fig. 1) composition is used, and concrete structure is as follows:
This device comprises reactor 4, is arranged on the well heater 1 of these reactor 4 bottoms, and its effect is to make unstripped gas and recirculated water reach suitable preheating temperature, passes through the sleeve pipe 5 of beds 3 and reactor 4 outer setting more from bottom to up; Be provided with heating medium (stack gas) pipeline in the described well heater 1, the inlet 18 of this flue gas duct is opened in the top of well heater, the outlet 19 of flue gas duct is opened in the bottom of well heater, the recirculated water that will enter in the well heater by flue gas duct heats, offer this recirculated water inlet 16 and recirculated water on the wall of well heater respectively and go out 17, circulating water outlet 17 is opened in the top of well heater, and communicates with described reactor 4 sleeve pipe 5 outward; Be provided with the unstripped gas pipeline in the described well heater 4, the outlet 13 of the inlet 12 of the unstripped gas pipeline of well heater 4 and the unstripped gas pipeline of well heater 4 is arranged on the wall of well heater 4, the outlet 13 of the unstripped gas pipeline of this well heater 4 is connected with the unstripped gas of described reactor inlet 14, logical superheated recirculated water is heated to suitable preheating temperature with the ducted unstripped gas of unstripped gas, and the back enters reactor reaction by the outlet 13 of the unstripped gas pipeline of well heater and the unstripped gas inlet 14 of reactor.
Products export 21 places of the bottom of reactor 4 also are connected with product collector 22 and product groove 27 successively, this product collector 22 is to be used for being collected in reacting the product that the boiling point that generates is higher than temperature of reaction in this reactor, and this product groove 27 is to be used for collecting the product that transports out from this product collector.The top of reactor 4 is connected with the interchanger 23 of tool condensation and the triphase separator 24 of tool centrifugation successively, the product that reaction is generated is flowed through behind this interchanger 23 and the triphase separator 24, elder generation's condensation, to sift out liquid hydrocarbon product and unconverted synthetic gas, in this triphase separator 24, the lower hydro carbons of above-mentioned boiling point and water and unconverted synthetic gas are carried out water again, oil phase and gas phase separation, oil phase can be sent in the described product groove 27 as the cryogenic condensation product after reducing pressure, gas phase then enters and continues reaction in next bank of reactor, so that the reaction of unstripped gas is more abundant.
The said fixing bed apparatus also is provided with waste gas inlet 18 and flue gas outlet 19 on the wall of well heater 1, waste gas inlet 18 is on the top of well heater, and flue gas outlet 19 is used for making the recirculated water of well heater 1 inside to be heated to preset temperature in the bottom.
Top at the sleeve pipe 5 of reactor 4 peripheral hardwares also is connected with water tank 7, is used for storage effusive recirculated water from this sleeve pipe 5, and this water tank 7 can be regulated temperature, pressure and the liquid level of described recirculated water in time.Also be provided with liquidometer 8, turnover valve 9 (and more preferably also being provided with explosion trap (or claiming safety valve) 10) on this water tank 7, eliminate because the excessive too fast potential safety hazard of hydraulic pressure rising that causes of heat absorption with timely in order to the situation of level monitoring.
Described water tank 7 lower ends be provided with well heater 1 on recirculated water inlet 16 circulation lines that communicate offered, when recirculated water rises to water tank 7, temperature descended after itself and the external world carried out heat exchange, then because the effect of gravity or recycle pump 2, and under the control of recirculated water control valve 11, from the circulation line of outside, flow down to reenter sleeve bottom, begin circulation.
The gas that comes out from reactor 4 tops comprises the light hydrocarbon product of unreacted unstripped gas and generation, its temperature is still very high, and after interchanger (condensation) 23 condensations, temperature approaches room temperature, enter in the triphase separator 24 that is connected with interchanger 23, wherein lower carbon number hydrocarbons (the CH of minute quantity
4Deng) and the unreacted unstripped gas of sub-fraction continue reaction through entering second bank of reactor, second group of tail gas discharged through interchanger 23 and triphase separator 24 backs by 28 emptying of tail gas blow-off valve or as heating fuel.The liquid phase substance of discharging in the triphase separator 24 comprises water two portions of liquefied hydrocarbon and generation, wherein liquefied hydrocarbon enters product collector 25, send into product groove 27 after the decompression and carry out deep processing, water enters water collector 26 (being also referred to as the reaction water medial launder), goes rectifying to reclaim the unit with the oxygen-bearing organic matter in the recycle-water afterwards.The boiling point that generates in the reaction then because the effect of self gravitation enters product collector 22 (also claiming cryogenic condensation thing medial launder), send product groove 27 to carry out deep processing than the high heavy hydrocarbons of temperature of reaction after decompression.
Embodiment two:
As shown in Figures 2 and 3, it is the fixed bed device that Fischer-Tropsch synthesis that two groups of multitubular reactors are formed is used, be that with the different of Fig. 1 every bank of reactor 4 is multitube (air delivering pipeline) fixed beds, this multitube (air delivering pipeline) vertically is arranged in above the gas distribution grid 20 that the lower end of reactor 4 is provided with, and adopt circulation line II to utilize recycle pump that recirculated water is carried out pump circulation, recirculated water is flowed fast, the recirculated water temperature difference is littler, be more conducive to Fischer-Tropsch synthesis, and adopt multitube fixed bed production ability bigger.Come out from reactor tail gas outlet 15 at gas, enter and enter second bank of reactor continuation reaction after second bank of reactor 4 also will be passed through condenser 23, three-phase product separator 24 before again, purpose is to separate the hydro carbons that enters in second bank of reactor, 4 gases, reduce the influence of hydrocarbon product to Fischer-Tropsch synthesis, increase the dividing potential drop of unconverted synthesis gas and light hydrocarbon gas, help improving the transformation efficiency and the selectivity of second bank of reactor 4.Whole device flow process is basic identical with embodiment one, and device moves more than a year, in order.The CO per pass conversion reaches 80%, C
5 +Selectivity reach more than 80%.Though this scheme has increased the cost of reactor, reduced the investment of tail gas tripping device and power set, enlarged production capacity, increased benefit, and can continue to increase the number of reactor according to reaction needed.
The advantage of utilizing fixed bed device of the present utility model to carry out fischer-tropsch reaction is:
(1) unstripped gas can carry out heat exchange in circulating water heater, has reached the reasonable utilization of energy.
(2) with heat transferring medium water reactor is carried out heat-obtaining and concurrent heating, the bigger characteristics of thermal capacitance of water have been utilized fully, and can choose from thermal cycle I and two kinds of different modes of high-pressure pump forced circulation II according to the difference of reaction condition, and can at any time regulate the flow of pump, can make a large amount of the shifting out of reaction heat, keep the temperature substantially constant of reaction, so the reaction system scope that the utility model was suitable for is extremely wide.
(3) the water tank height of level monitoring at any time, and carry out as required the adjusting of the water yield, and safety valve has certain pressure limit, and automatically overvoltage emptying has guaranteed the safe operation of device.
(4) directly product is carried out primary separation according to the difference of boiling point, for follow-up product purification is prepared, and water has been carried out rectifying recovery, energy-conserving and environment-protective.
(5) tail gas does not circulate, but directly emptying or act as a fuel is burnt, and has reduced power set, saved investment, and operation is simple, is applicable to the Fischer-Tropsch synthesizer of middle-size and small-size scale.
(6) this scheme practical application has moved more than a year, the fault of parking never occurs causing because of technology or Equipment.
(7) conversion per pass of CO reaches 80%, C5 +Selectively be not less than 80%.
(8) this programme also can continue to increase the 3rd group or more group reaction devices, each group reaction device cascade reaction wherein, after every group of product that comes out removed liquid hydrocarbon through condensation separation, tail gas entered next group reaction device and continues reaction, until the synthesis gas conversion ratio reaches higher level.
Claims (10)
1. fixed bed device that is used for Fischer-Tropsch synthesis, it is characterized in that: it is made up of this fixed bed device the fixed bed that two groups of head and the tail are contacted mutually at least, every group of fixed bed includes reactor, the corresponding well heater that is connected with this reactor, the sleeve pipe that joins with this well heater, interchanger and triphase separator, wherein, be provided with unstripped gas pipeline and heating medium pipeline in the well heater of every group of fixed bed, the wall of well heater is provided with unstripped gas inlet and unstripped gas outlet, this unstripped gas outlet is connected with this bank of reactor, also be provided with the heating medium inlet on the well heater wall, the heating medium outlet, and the recirculated water of well heater inlet and circulating water outlet, the circulating water outlet of every group of well heater communicates with this group sleeve pipe, all is connected with interchanger and triphase separator successively between the reactor of described two groups of polyphones.
2. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 1, it is characterized in that: this recirculated water inlet is opened in the bottom of the wall of well heater, circulating water outlet is opened in the top of the wall of well heater, and this circulating water outlet communicates with described sleeve pipe.
3. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 1 is characterized in that: the bottom of described each bank of reactor all is connected with product collector and product groove successively.
4. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 3 is characterized in that: the top of described each bank of reactor all is connected with interchanger, triphase separator.
5. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 1, it is characterized in that: the inner heating medium pipeline that is provided with of described well heater is a flue gas duct, described heating medium inlet is the inlet of flue gas duct, and the heating medium outlet is the outlet of flue gas duct.
6. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 1 is characterized in that: described telescopic top is provided with circulating water outlet, and this sleeve pipe also is connected with the water tank that is used for storing effusive recirculated water from this sleeve pipe by circulating water outlet.
7. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 6 is characterized in that: described water tank is provided with liquidometer and/or turnover valve.
8. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 7 is characterized in that: also be provided with explosion trap on the described water tank.
9. the fixed bed device that is used for Fischer-Tropsch synthesis as claimed in claim 6, it is characterized in that: described water tank is provided with the circulation line that communicates with the recirculated water inlet offered on the well heater, and this circulation line be the natural circulation pipeline and the cycle of higher pressure pipeline of parallel connection.
10. as each described fixed bed device that is used for Fischer-Tropsch synthesis of claim 1-9, it is characterized in that: unstripped gas pipeline and heating medium pipeline are spiral pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201495897U CN201058854Y (en) | 2007-06-13 | 2007-06-13 | Fixed bed device for F-T synthesis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201495897U CN201058854Y (en) | 2007-06-13 | 2007-06-13 | Fixed bed device for F-T synthesis |
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| CN201058854Y true CN201058854Y (en) | 2008-05-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2007201495897U Expired - Lifetime CN201058854Y (en) | 2007-06-13 | 2007-06-13 | Fixed bed device for F-T synthesis |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102441351A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Slurry bed Fischer-Tropsch synthetic reactor |
| CN102861539A (en) * | 2011-07-04 | 2013-01-09 | 中国石油化工股份有限公司 | Novel slurry bed ft synthesis reactor |
| CN102861540A (en) * | 2011-07-04 | 2013-01-09 | 中国石油化工股份有限公司 | Slurry bed ft synthesis reactor |
-
2007
- 2007-06-13 CN CNU2007201495897U patent/CN201058854Y/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102441351A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Slurry bed Fischer-Tropsch synthetic reactor |
| CN102441351B (en) * | 2010-10-12 | 2015-09-02 | 中国石油化工股份有限公司 | A kind of slurry bed ft synthetic reactor |
| CN102861539A (en) * | 2011-07-04 | 2013-01-09 | 中国石油化工股份有限公司 | Novel slurry bed ft synthesis reactor |
| CN102861540A (en) * | 2011-07-04 | 2013-01-09 | 中国石油化工股份有限公司 | Slurry bed ft synthesis reactor |
| CN102861540B (en) * | 2011-07-04 | 2015-12-02 | 中国石油化工股份有限公司 | A kind of slurry bed ft synthetic reactor |
| CN102861539B (en) * | 2011-07-04 | 2016-03-02 | 中国石油化工股份有限公司 | A kind of slurry bed ft synthetic reactor |
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