CN202808648U - Methanol synthetic system - Google Patents

Abstract

The utility model discloses a methanol synthetic system. The system comprises a gas-solid phase catalytic reactor and a separator, wherein the gas-solid phase catalytic reactor is provided with a reaction gas inlet, a reaction generated gas outlet, a boiler water feed inlet and a byproduct steam outlet; a reaction generated gas inlet communicated with the reaction generated gas outlet of the gas-solid phase catalytic reactor is arranged on the side wall of the separator, a liquid phase output pipe is disposed at the bottom, and a recycle gas outlet is positioned at the top; and the recycle gas outlet of the separator is connected with a condenser, and a recycle gas outlet of the condenser is communicated with the reaction gas inlet of the gas-solid phase catalytic reactor. According to the technical scheme, the separator is communicated with the condenser, namely, recycle gas departing from the separator is not mixed with synthesis gas as in the prior art but enters the condenser for cooling, part of methanol is separated, therefore waxiness during synthesis of the methanol is reduced, and stable yield of the methanol is maintained simultaneously.

Description

System for methanol synthesis

Technical field

The utility model relates to technical field of chemical synthesis, in particular to a kind of system for methanol synthesis.

Background technology

In chemical process, usually because the synthesis reactor reaction bed temperature is uneven, temperature of reaction is too high or cross reaction temperature and spend the uppity factor of reactor catalyst bed temperature such as low and cause by product too much.

For, ammonia synthesis and CO conversion this class gas-solid synthetic by the lower methylamine of pressurization, methyl ether, methyl alcohol exothermic catalytic reaction mutually, along with the carrying out of reaction, the reaction heat of constantly emitting improves reaction bed temperature.In order to reduce the efficient of by product and raising reactor, need to shift out reaction heat so that temperature of reaction is in a rational scope.In industrial reactor, once widely used a kind of be the multistage insulation reaction, reduce the reaction gas temperature with the unstripped gas Quench between two sections, this reactor has also reduced reactant concn during because of the unstripped gas Quench when reducing the reaction gas temperature, affected combined coefficient.The another kind of shell and tube reactor that is used for the synthetic Lurgi company of methyl alcohol, many pipes on having in housing between lower tubesheet are equipped with catalyzer in the pipe, unstripped gas enters from the top inlet mouth and is distributed to each pipe, synthesizing methanol in the in-built catalyst layer of pipe, lateral inflow between pipe.Reaction tubes is managed outer boiled water and is continuously removed heat, produces steam and is gone out by the side pipe, and reaction gas goes out tower by the bottom escape pipe, and this tower has a narrow range of temperature, but the catalyst filling coefficient is little.

The methyl alcohol synthetic technology of another kind of DAVY company exploitation, its synthesis reactor structural representation as shown in Figure 1, catalyst loading produces middle pressure steam at the shell-side of reactor 100 ' in the heat transfer tube 130 '.Fresh synthetic gas enters from the pipe core 120 ' of reactor 100 ' bottom, dispensing orifice is arranged to guarantee being evenly distributed of gas on the pipe core 120 ' tube wall.Gas radially passes through the beds 110 ' of reactor 100 ' from inside to outside.Then upwards flow in the bottom that the feedwater that comes from drum enters reactor 100 ' and the reaction heat that the methyl alcohol building-up reactions produces is taken away in the part vaporization.Temperature of reaction is regulated by the pressure of steam in the heat transfer tube 130 '.This technology can be with temperature of reaction control within the specific limits, and the expansion of reactor 100 ' throughput can realize by lengthening reactor length, aspect the maximization of methyl alcohol synthesis device its technical superiority is being arranged, extensively adopted by the synthetic producer of methyl alcohol gradually at present, but itself also exists some shortcomings.

Existing DAVY technology synthesis flow synoptic diagram, as depicted in figs. 1 and 2, wherein, reactive system comprises reactor 100 ', drum 200 ', the first synthesis loop intermediate heat 601 ', the second synthesis loop intermediate heat 602 ', water cooler 300 ', 400 ', synthesic gas compressor 501 ', recycle gas compressor 502 ', the first methanol separator 603 ', the second methanol separator 604 ', methyl alcohol flash drum 605 ' etc., fresh synthetic gas enters from the pipe core 120 ' of reactor 100 ' bottom, dispensing orifice is arranged to guarantee being evenly distributed of gas on the pipe core 120 ' tube wall.Gas radially passes through the beds 110 ' of reactor 100 ' from inside to outside.Because fresh synthetic gas enters from the pipe core 120 ' of reactor 100 ' bottom, so at first radially entering into reactor 100 ' middle and lower part beds 110 ' from inside to outside by the dispensing orifice on reactor 100 ' the middle and lower part pipe core 120 ' tube wall, the larger proportion synthetic gas reacts; Along pipe core 120 ' more up, synthetic gas is just thinner, namely reactor 100 ' lower catalyst bed layer 110 ' just has more synthetic gas and participates in reaction for reactor 100 ' upper catalyst bed layer 110 ', and the activity of reactor 100 ' lower catalytic agent will descend sooner with respect to the activity of reactor 100 ' top catalyzer like this.Like this, when having arrived the middle and later periods in catalyzer work-ing life, entering major part in the synthetic gas of dispensing orifice on reactor 100 ' the lower central pipe 120 ' tube wall radially enters into from inside to outside and does not have enough time to carry out chemical reaction toward contact behind reactor 100 ' the lower catalyst bed layer 110 ' and just left beds 110 ', again because the synthetic gas ratio middle and upper part of reacting in reactor 100 ' bottom all large, even the transformation efficiency at the catalyzer place that the activity of synthetic gas on reactor 100 ' top is higher also keeps higher level, but because the synthetic tolerance less on reactor 100 ' top, so that the per pass conversion of synthesis gas reaction methanol will descend rapidly generally, so that methanol output also can descend thereupon; If the maintenance methanol output just needs to strengthen internal circulating load and the cycle index of unreacted synthetic gas, this has increased again energy consumption undoubtedly.When the middle and later periods in catalyzer work-ing life, if adopt the method that significantly improves beds 110 ' temperature to improve the activity of catalyzer, catalyzer faster decline in work-ing life can be made on the one hand, more wax (especially when bed temperature is higher than more than 280 ℃) can be produced on the other hand.Like this, often originally can use the time of the bed catalyst change of long or longer time greatly to shift to an earlier date, and the catalyzer that also keeps greater activity on reactor 100 ' top is also together changed (when the methanol synthesis catalyst crossed of normal operation is changed with the catalyzer that reactor 100 ' bottom almost can't be used, the catalyzer of integral reactor 100 ' all and contact with air, in case in air atmosphere, still activated catalyzer also will damage and can't use because poisoning fast), caused economically waste.

In the existing DAVY technology, methyl alcohol synthetic reactor is radial flow reactors, top in synthesis reactor, hot gas needs could flow out outside the tower behind the downward baffling, residence time is longer in tower, cause the speed that shifts out reaction heat to shift out speed than the reaction heat of other positions of beds and want slow, so that local overheating usually appears in the reactor catalyst bed, especially when bed temperature is higher than 280 ℃, tend to produce a large amount of wax, so that catalyst activity is accelerated decay, indirectly cause the waste of catalyzer simultaneously.

In the existing DAVY technology, oiler feed in the drum all enters heat transfer tube from the bottom of reactor, become steam cycle back-steam bag after the absorption reaction heat, like this, oiler feed a large amount of absorption reaction heat vaporization when the reactor middle and lower part that temperature is lower forms high-temperature steam, these high-temperature steams and near the ability oiler feed lower far below temperature of the high-temperature boiler of reaction bed temperature feedwater absorbing heat, so that the reaction heat that reactor top produces can not in time be pulled away, often cause the temperature on reactor catalyst bed top greatly to exceed the temperature of reactor catalyst bed middle and lower part.

At present, DAVY technology synthesizing methanol flow process, can carry out according to flow process shown in Figure 2, synthetic virgin gas enters synthesic gas compressor 501 ' and compresses, and the circulation gas that most of virgin gas and the second methanol separator 604 ' come after the 501 ' supercharging of process synthesic gas compressor mixes the formation gas mixture; Then gas mixture enters the first synthesis reactor 100 ' after the preheating first in the first synthesis loop intermediate heat 601 ', in the first synthesis reactor 100 ', the methyl alcohol building-up reactions is carried out under highly active copper-based catalysts effect, and this reaction is thermopositive reaction, reaction heat by-product low-pressure steam; Reaction generates carries out preheating to wanting into the gas mixture of tower through the first synthesis loop intermediate heat 601 ' after gas leaves the first synthesis reactor 100 ', then enters water cooler 300 ' and cools off; Circulation gas in the reaction generation gas enters the first methanol separator 603 ' with thick methyl alcohol to be separated.Isolated circulation gas and enter in addition recycle gas compressor 502 ' after the fresh synthesis gas mixing of part after synthetic air compressor 501 ' supercharging and enter again preheating in the second synthesis loop intermediate heat 602 ' after compressed in the first methanol separator 603 ', then enter the second synthesis reactor, the same by-product low-pressure steam of the second synthesis reactor, after the reaction of leaving the second synthesis reactor generates gas 602 ' preheating enters the inlet tower gas of the second synthesis reactor in advance through the second synthesis loop intermediate heat, enter the second water cooler 400 ', reaction generates in the gas in the second water cooler 400 circulation gas and thick methyl alcohol enter the second methanol separator 604 ', and isolated thick methyl alcohol removes methyl alcohol flash drum 605 ' through behind the filter in the first methanol separator 603 ' and the second methanol separator 604 '.In the second methanol separator 604 ' major part of isolated circulation gas with enter synthesic gas compressor 501 ' after synthetic virgin gas is mixed.Simultaneously, need emit a part of off-gas to keep the rare gas elementes such as methane in the circulation gas and nitrogen within certain concentration range.

In methanol production process, usually because the too high by product that causes of methanol content is too much in the reaction gas, have influence on normal production.

In the existing DAVY technology, the part fresh synthesis gas with enter the recycle gas compressor pressurization after circulation gas from one of them thick separating methanol tank mixes after, after the heating of synthesis loop intermediate heat, enter methanol sythesis reactor 100 ' and carry out the methyl alcohol building-up reactions; Because residual in the circulation gas have part methyl alcohol, the too high meeting of methanol content causes the growing amount of wax in the building-up process to increase, and methanol output also can descend thereupon; If the maintenance methanol output just needs to strengthen internal circulating load and the cycle index of unreacted synthetic gas, this has increased again energy consumption undoubtedly.

The utility model content

The utility model aims to provide a kind of system for methanol synthesis, to solve the too high technical problem of circulation gas methanol content in the prior art system for methanol synthesis.

To achieve these goals, according to an aspect of the present utility model, provide a kind of system for methanol synthesis.This system for methanol synthesis, comprise: gas solid catalytic reactor, be provided with reaction gas entrance and reaction and generate the gas outlet, oiler feed entrance and byproduct steam outlet, separator is provided with reaction and generates the gas entrance on the sidewall, the bottom is provided with the liquid phase output tube, the top is provided with the circulation gas outlet, and reaction generates the gas entrance and communicates with the reaction generation gas outlet of gas solid catalytic reactor; The circulation gas outlet of separator links to each other with condenser, and the circulation gas relief outlet of condenser communicates with the reaction gas entrance of gas solid catalytic reactor.

Further, also be provided with gas compressor between the outlet of the circulation gas of separator and the condenser.

Further, separator is connected with the cooling air pipeline, and condenser is provided with condensation of gas medium inlet pipe and gas cooling medium outlet pipe, and system for methanol synthesis further comprises:

Further, be connected with the cooling air pipeline of separator and the condensation of gas medium inlet pipe of condenser respectively by power set.

Further, air filter is connected with respectively room air pipeline and ambient air pipeline, is respectively arranged with gas flow control valve on room air pipeline and the ambient air pipeline.

Further, comprise two gas solid catalytic reactors and the separator that is arranged in parallel.

Further, gas solid catalytic reactor comprises: reactor shell is formed with the gas inlet pipeline that extends along the sidewall tangential direction on its sidewall; Beds is arranged in the reactor shell, and forms the eddy flow chamber of ring-type between the reactor shell, and beds is hollow circular cylinder, is provided with the through hole that the eddy flow chamber is communicated with beds inside on the sidewall of beds; And heat-exchanger rig, be arranged in the beds.

Further, heat-exchanger rig comprises many heat transfer tubes that are arranged on equably in the beds, and wherein, the flow direction of medium is opposite with the flow direction of the interior medium of heat transfer tube of remainder in the part heat transfer tube; System for methanol synthesis also comprises the drum that communicates with heat transfer tube, is provided with variable valve on the back with water inlet line of the part heat transfer tube that the water in the drum enters from bottom to top; Be provided with thermopair near the inherent heat transfer tube of beds, the control loop of the flow of water in variable valve and the thermopair formation control heat transfer tube.

Further, be provided with on the back with water inlet line of the part heat transfer tube that the water in the drum enters from top to bottom for the variable frequency pump of regulating hydraulic pressure, the exit end of this part heat transfer tube and the exit end of variable frequency pump are respectively arranged with differential manometer, and differential manometer and variable frequency pump form and suppress the control loop that steam flows backwards.

Further, separator comprises: the lime set withdrawing can, upright radiator is arranged side by side at the top of lime set withdrawing can with the scum dredger tank, and all is connected with the lime set withdrawing can.

Further, condenser comprises: elementary vertical (type) condenser comprises elementary vertical (type) condenser shell side and is arranged on the interior elementary vertical (type) condenser tube side of elementary vertical (type) condenser shell side; Secondary vertical (type) condenser, comprise secondary vertical (type) condenser shell side and be arranged on the interior secondary vertical (type) condenser tube side of secondary vertical (type) condenser shell side, secondary vertical (type) condenser is arranged on the top of elementary vertical (type) condenser, and elementary vertical (type) condenser tube side and secondary vertical (type) condenser tube side are connected, and elementary vertical (type) condenser top is provided with the distance piece that separates for elementary vertical (type) condenser shell side and secondary vertical (type) condenser shell side; And condenser lime set tank, be arranged on the bottom of elementary vertical (type) condenser, communicate with elementary vertical (type) condenser tube side.

Further, gas compressor comprises synthesic gas compressor and recycle gas compressor, synthesic gas compressor is provided with fresh synthesis gas entrance and fresh synthesis gas outlet, and synthesic gas compressor is connected with purified synthesis gas preheater, purified synthesis gas groove, synthesis loop intermediate heat, gas solid catalytic reactor successively by syngas outlet; The reaction of gas solid catalytic reactor generates the gas outlet and is connected with synthesis loop intermediate heat, thick methyl alcohol air cooler, separator successively; The circulation gas outlet of separator is connected with recycle gas compressor, condenser, circulating gas preheater, synthesis loop intermediate heat, gas solid catalytic reactor successively.

Use the technical solution of the utility model, separator is connected with condenser, the circulation gas that namely leaves separator does not mix with synthetic gas as prior art, lower the temperature but enter condenser, cutting out partial methyl alcohol, thereby be conducive to reduce the formation of wax in the synthesizing methanol process, also be conducive to keep the stable of methanol output simultaneously.Under equal air input, same composition, the equal filling condition of catalyzer and duration of service same period condition because more thick methanol product in the reactor is removed in condenser, therefore, the wax of generation still less, the methane of generation still less, methanol output is larger.

Description of drawings

Figure of description is used to provide further understanding of the present utility model, consists of a part of the present utility model, and illustrative examples of the present utility model and explanation thereof are used for explaining the utility model, do not consist of improper restriction of the present utility model.In the accompanying drawings:

Fig. 1 shows the structural representation of existing davy technology synthesis reactor;

Fig. 2 shows the synthetic schematic flow sheet of existing davy technology;

Fig. 3 shows system for methanol synthesis structure and the schematic flow sheet according to the utility model embodiment;

Fig. 4 shows the gas solid catalytic reactor sectional elevation structural representation according to the utility model embodiment;

Fig. 5 shows the A-A cross section plan structure synoptic diagram according to Fig. 4;

Fig. 6 shows the arrangement synoptic diagram of heat transfer tube in gas solid catalytic reactor according to the utility model embodiment;

Fig. 7 shows the gas solid catalytic reactor structural representation according to the utility model embodiment;

Fig. 8 shows gas inlet, B-B cross section pipeline according to Fig. 7 and look up structural representation on gas solid catalytic reactor;

Fig. 9 shows the plan structure synoptic diagram of gas inlet, C-C cross section pipeline on gas solid catalytic reactor according to Fig. 7;

Figure 10 shows the structural representation according to the automatic control loop of the flow of water in the variable valve of the utility model embodiment and the thermopair formation control heat transfer tube;

Figure 11 shows the sectional structure synoptic diagram according to the separator of the utility model embodiment;

Figure 12 shows the plan structure synoptic diagram according to the separator of the utility model embodiment;

Figure 13 shows the structural representation according to the condenser of the utility model embodiment; And

Figure 14 shows system for methanol synthesis structure and the schematic flow sheet according to another embodiment of the utility model.

Embodiment

Need to prove that in the situation of not conflicting, embodiment and the feature among the embodiment in the utility model can make up mutually.Describe below with reference to the accompanying drawings and in conjunction with the embodiments the utility model in detail.

System for methanol synthesis of the present utility model is particularly suitable for the methyl alcohol synthetic reaction process, also can be used for the chemical processes such as methyl ether, methylamine, methyl ether, ammonia synthesis and CO conversion.

According to a kind of typical embodiment of the utility model, system for methanol synthesis comprises gas solid catalytic reactor 100, separator 600 and condenser 400 as shown in Figure 3, wherein, gas solid catalytic reactor 100 is provided with the reaction gas entrance and should generates the gas outlet, oiler feed entrance and byproduct steam outlet, be provided with reaction on separator 600 sidewalls and generate the gas entrance, the bottom is provided with the liquid phase output tube, the top is provided with the circulation gas outlet, and reaction generates the gas entrance and communicates with the reaction generation gas outlet of gas solid catalytic reactor 100; The circulation gas outlet of separator 600 links to each other with condenser 400, and the circulation gas relief outlet of condenser 400 communicates with the reaction gas entrance of gas solid catalytic reactor 100.Use the technical solution of the utility model, separator 600 is connected with condenser, the circulation gas that namely leaves separator 600 does not just mix with fresh synthesis gas as prior art at once, lower the temperature but be introduced into condenser, Re-isolation goes out part methyl alcohol, thereby be conducive to reduce the formation of wax in the synthesizing methanol process, also be conducive to keep the stable of methanol output simultaneously.Under equal air input, same composition, the equal filling condition of catalyzer and duration of service same period condition because more thick methanol product in the reactor is removed in condenser, therefore, the wax of generation still less, the methane of generation still less, methanol output is larger.Preferably, also be provided with gas compressor 500 between the outlet of the circulation gas of separator 600 and the condenser 400, this gas compressor 500 comprises synthesic gas compressor 501 and recycle gas compressor 502.

Preferably, be provided with the cooling air pipeline in the separator 600, condenser 400 is provided with condensation of gas medium inlet pipe and gas cooling medium outlet pipe, system for methanol synthesis further comprises air filter 700, and air filter 700 is connected with the cooling air pipeline of separator 600 and the condensation of gas medium inlet pipe of condenser 400 respectively by power set 701.Airborne dust and part water filtration can be removed like this, be conducive to the equipment long-term operation.Preferably, air filter is connected with respectively room air pipeline 702 and ambient air pipeline, be respectively arranged with gas flow control valve on room air pipeline 702 and the ambient air pipeline 703, thus the temperature of being convenient to and regulating cooling air with the flow of regulating both.Wherein, power set 701 can be gas blower.Wherein, ambient air is outside air.Room air and ambient air are that outside air filters dust removal dust and part water through air filter first, are that each above user (separator upright radiator and condenser) carries tempering air by gas blower then; Room air and ambient air have variable valve on the pipeline separately, can adjust the tempering air temperature by the flow of regulating both.In addition, the tempering air of being carried by gas blower also can be the relevant logistics of thick methanol stripper non-condensable gas, residual solution gas and low-boiling-point substance system cools.

According to embodiment of the present utility model, as shown in Figure 3, gas solid catalytic reactor 100 reaction generation gas outlets generate the gas entrances with 801 reactions of synthesis loop intermediate heat and are connected, and the 801 reaction generation gas outlets of synthesis loop intermediate heat generate the gas entrance with thick methyl alcohol air cooler 300 reactions and are connected.Pass through 801 heat exchange of synthesis loop intermediate heat from gas solid catalytic reactor 100 reaction generation gas and fresh synthesis gas, circulation gas out, reaction generates the temperature degree and descends, fresh synthesis gas and circulation gas temperature rise to suitable temperature of reaction, and (reaction needed is carried out in the suitable range of reaction temperature of this area routine, if it is excessively low that fresh synthesis gas and circulation gas enter the temperature of reactor, also can cause increasing of side reaction by-products so that temperature of reaction is low; Temperature of reaction is too high equally also can cause increasing of side reaction by-products), thick methyl alcohol air cooler 300 reaction generation gas outlets generate the gas entrance with separator 600 reactions and are connected, separator 600 circulation gas (leave reaction behind the separator 600 generate gas because also will be used for after separating thick methyl alcohol circulation again reaction so all be called circulation gas at this) export and be connected with recycle gas compressor 502 inlet mouths, recycle gas compressor 502 air outlets and condenser 400 circulation gas entrances are connected, the outlet of condenser 400 circulation gas is connected with circulating gas preheater 803 circulation gas entrances, and the outlet of circulating gas preheater 803 circulation gas is connected and is connected with synthesis loop intermediate heat 801 circulation gas entrances with the outlet of purified synthesis gas groove.Before entering synthesis loop intermediate heat 801, circulation gas leaves behind the circulating gas preheater 803 and merges into one gas from purified synthesis gas groove fresh synthesis gas out.Pass through 801 heat exchange of synthesis loop intermediate heat from gas solid catalytic reactor 100 reaction generation gas and fresh synthesis gas, circulation gas out, reaction generates the temperature degree and descends, fresh synthesis gas and circulation gas temperature rise, and the outlet of synthesis loop intermediate heat 801 circulation gas is connected with gas solid catalytic reactor 100 entrances.

In the prior art, what usually adopt is the series-parallel mode of reactor, as long as wherein a tower stops, because circulation can't be carried out, react unbalance fast, usually cause an other tower to stop, cause the interlock shutdown of other upstream and downstream devices or the synthetic gas emptying of upstream, cause and greatly lose and waste.According to a kind of typical embodiment of the utility model, system for methanol synthesis comprises two gas solid catalytic reactors 100 and the separator 600 that is arranged in parallel.Be conducive to like this reduce facility investment, be conducive to maintenance, keep the continuity that other devices are produced, avoid the loss that causes because of parking.Certainly, system for methanol synthesis of the present utility model also can be two the public cover separators of reactors, thick methyl alcohol air cooler 300 and synthesis loop intermediate heats 801.According to another typical embodiment of the utility model, as shown in figure 14, two gas solid catalytic reactors 100 that are arranged in parallel can be public a cover separator 600, thick methyl alcohol air cooler 300 and synthesis loop intermediate heat 801.

According to the utility model one exemplary embodiments, as shown in Figure 4, gas solid catalytic reactor 100 comprises reactor shell 101, beds 110 and heat-exchanger rig, wherein, is formed with the gas inlet pipeline 150 that extends along the sidewall tangential direction on the sidewall of reactor shell 101; Beds 110 is arranged in the reactor shell 101, and form the eddy flow chamber 140 of ring-type between the reactor shell 101, beds 110 is hollow circular cylinder, be provided with the through hole 111 that communicates with beds 110 inside on the sidewall of beds 110, heat-exchanger rig is arranged in the beds 110.

Gas solid catalytic reactor 100 of the present utility model, has the eddy flow chamber 140 that the housing by the reactor shell 101 of the housing periphery that is set in beds 110 and beds 110 forms, eddy flow chamber 140 communicates with beds 110 inside by the through hole 111 that arranges on beds 110 housings, and the gas inlet pipeline 150 in eddy flow chamber 140 arranges along the sidewall tangential direction of reactor shell 101, so that reaction gas enters eddy flow chamber 140 by gas inlet pipeline 150 along eddy flow chamber 140 tangential direction.To be close to the reactor shell inwall after reaction gas tangentially enters and do the circumference swirling motion, then reaction gas both direction diffusion eddy flow up and down in the process of circumference eddy flow, the reaction gas tangential admission will obtain the longer residence time in the mode of eddy flow chamber inward eddy with respect to the mode of direct radial air inlet, to there be the longer time in the eddy flow chamber, to enter beds by through hole again after the even eddy flow diffusion and under the effect of catalyzer, react, so that reaction gas more evenly distributes in the whole beds axial space of reactor.Gas solid catalytic reactor of the present utility model is particularly suitable for the methyl alcohol synthetic reaction process, also can be used for the chemical processes such as methyl ether, methylamine, methyl ether, ammonia synthesis and CO conversion.

According to the utility model one exemplary embodiments, as shown in Figure 4, be provided with pipe core 120 on the axis of beds 110, be provided with equably pipe core gas collection hole 121 on the tube wall of pipe core 120, pipe core is both ends open formation reaction generation gas outlet 122 about in the of 120.Reaction gas enters eddy flow chamber 140 after the even distribution of axial space, enters beds 110 by the through hole 111 that arranges on beds 110 housings, and reaction gas is radially from inside to outside by beds 110.Reaction gas forms reaction and generates gas (containing the reaction gas that reacts) and radially enter in the pipe core 120 by pipe core gas collection hole 121 behind the partial reaction under the effect of catalyzer, then reaction generates gas and generates gas outlet 122 from the reaction at two ends up and down and leave reactor.According to the utility model one typical embodiment, after reaction generation gas outlet 122 two strands of synthetic gas that leave reactor at two ends converge up and down, enter the reaction gas that 801 preheatings of synthesis loop intermediate heat are about to enter reactor.

Preferably, shown in Fig. 5,6, the gas inlet pipeline 150 of reactor comprises many, the height location of each gas inlet pipeline 150 is identical or different, and each gas inlet pipeline 150 is centered around the periphery of reactor shell 101 equably in the projection of overlooking direction, so that reaction gas more evenly distributes in eddy flow chamber 140.

Preferably, shown in Fig. 7-10, the gas inlet pipeline 150 of reactor comprises the first gas inlet pipeline 151, the second gas inlet pipeline 152, the 3rd gas inlet pipeline 153, and the 4th gas inlet pipeline 154, wherein, be arranged on 1/3 At The Height of beds 110 the first gas inlet pipeline 151 and the second gas inlet pipeline 152 centrosymmetry, be arranged on 2/3 At The Height of beds 110 the 3rd gas inlet pipeline 153 and the 4th gas inlet pipeline 154 centrosymmetry, so that reaction gas more evenly distributes in eddy flow chamber 140, and the synthetic gas that the reactor lower part beds can not occur entering in the prior art is greatly more than the situation of this synthetic gas skewness of synthetic gas that enters reactor upper catalyst bed layer.

Preferably, heat transfer tube 130 communicates with drum 200, the reaction heat that building-up reactions produces is taken away in the heat transfer tube 130 and the part vaporization that enter reactor from the next oiler feed of drum, and temperature of reaction can be regulated by the pressure of heat transfer tube 130 interior steam and the flow of oiler feed.According to the utility model one exemplary embodiments, heat-exchanger rig comprises many heat transfer tubes 130 that are arranged on equably in the beds 110, and wherein, the flow direction of part heat transfer tube 130 interior media is opposite with the flow direction of the heat transfer tube 130 interior media of remainder.Preferably, be provided with on the pipeline of the part heat transfer tube 130 that the water in the drum 200 enters from top to bottom for the multiphase pump of regulating hydraulic pressure, be preferably variable frequency pump 201, the exit end of this part heat transfer tube 130 and the exit end of multiphase pump are respectively arranged with differential manometer, and differential manometer and multiphase pump form and suppress the automatic control loop that steam falls to go here and there.Shown in Fig. 5,6, the heat transfer tube 131 usefulness white circle that water enters from bottom to top represent that the heat transfer tube 132 usefulness black circles that water enters represent from top to bottom.Like this, the reaction heat that existing drum 200 feedwater absorption reactor thermally Lower Halves from bottom to top produce has again top-down drum 200 feedwater to take the reaction heat that the reactor first half produces away.According to a kind of typical embodiment of the utility model, shown in Fig. 5,6, draw two oiler feed house stewards from the drum bottom, article one, the oiler feed house steward is divided into two-way, one the tunnel gives the first circumference set of heat exchange tubes, these road drum 200 feedwater enter the first circumference set of heat exchange tubes heat transfer tube from bottom to top, the 3rd circumference set of heat exchange tubes is given on another road, these road drum 200 feedwater enter the 3rd circumference set of heat exchange tubes heat transfer tube from bottom to top, part vaporization or all after the vaporization is left and is converged into one the tunnel after the first and third circumference set of heat exchange tubes and return drum and carry out vapor-liquid separation; Oiler feed among the second oiler feed house steward is rear via the multiphase pump pressurization first to be two-way, one the tunnel gives the second circumference set of heat exchange tubes, these road drum 200 feedwater enter the second circumference set of heat exchange tubes heat transfer tube from top to bottom, the 4th circumference set of heat exchange tubes is given on another road, these road drum 200 feedwater enter the 4th circumference set of heat exchange tubes heat transfer tube from top to bottom, after part vaporization or the whole vaporization, leave second, converging into one the tunnel after the four circumference set of heat exchange tubes returns drum and carries out vapor-liquid separation, this pipeline and multiphase pump outlet of returning drum is equipped with differential manometer, the pressure reduction of differential manometer and multiphase pump rotating speed form automatic control loop, the multiphase pump rotating speed is adjusted rotating speed according to differential manometer pressure reduction, constantly keep the multiphase pump top hole pressure to exceed second, four circumference set of heat exchange tubes top hole pressure certain limits, thus avoid steam to alter.Certainly, according to embodiment of the present utility model, heat transfer tube is not limited to four circumference set of heat exchange tubes, can be more groups.

Preferably, shown in Fig. 5,6, heat-exchanger rig comprises many groups centered by the axis of beds 110, rounded set of heat exchange tubes of arranging, each different set of heat exchange tubes of the flow direction of medium is spaced, and namely each set of heat exchange tubes is spaced by the flow direction of medium in it.The heat transfer tube spaced radial circumference uniform distribution that heat-eliminating medium flows is relatively arranged, so that the temperature variation of beds axial-radial all tends towards stability.

Preferably, as shown in Figure 6, heat-exchanger rig comprises many groups centered by the axis of beds 110, is spaced between the different heat transfer tube of the flow direction of medium in the rounded set of heat exchange tubes of arranging, set of heat exchange tubes.The heat transfer tube that heat-eliminating medium flows relatively is not that spaced radial is arranged, but arranges uniformly at intervals on same circumference, and this embodiment also can be so that the temperature of beds axial-radial be more even.

Preferably, drum 200 water enter on the pipeline of heat transfer tube 130 and are provided with variable valve 160, are provided with thermopair near the beds 110 inherent heat transfer tubes 130, the automatic control loop of variable valve 160 and the flow of thermopair formation control heat transfer tube 130 interior water.Further preferably, drum 200 forms the circulation path with heat transfer tube 130, and drum 200 water can be recycled, and drum is provided with blowdown pipeline and oiler feed moisturizing pipeline, but periodic blow down and in time fill into oiler feed, thereby keep in the drum oiler feed water quality good.

To sum up, adopt the gas solid catalytic reactor of the utility model preferred embodiment to have the following advantages:

1. the utility model gas solid catalytic reactor is with respect to the even distribution of the whole catalyst in reactor bed temperature of the easier realization of structure of reactor of the prior art, thereby avoided in the prior art because the synthesis reactor reaction bed temperature is uneven or temperature of reaction is too high or cross reaction temperature and spend the too much phenomenon of by product that causes such as low;

2. the easier regulation and control of the reaction bed temperature of the utility model gas solid catalytic reactor;

3. the expansion of the reactor throughput of the utility model gas solid catalytic reactor can also can realize with the method for widening pipe core by lengthening reactor length by strengthening reactor diameter, and is more flexible.

According to the typical embodiment of the utility model, shown in Figure 11,12, separator 600 comprises lime set withdrawing can 610, upright radiator 620 and scum dredger tank 630, wherein, upright radiator 620 is arranged side by side at the top of lime set withdrawing can 610 with scum dredger tank 630, and lime set withdrawing can 610 is connected with upright radiator 620 and scum dredger tank 630 respectively.During work, reaction generation gas 623 enters the heat-eliminating medium heat exchange cooling in upright radiator 620 tube sides and the shell side from top to bottom, the lime set that reaction generation air cooling but produces falls in the lime set withdrawing can 610, non-condensable gas then enters lime set withdrawing can 610 tops, and upwards baffling leaves separator 600 by the outlet of scum dredger tank 630 tops again.Wherein, water cooler adopts vertical structure, the wax that the reaction generation gas of high-voltage high-speed can get off condensation is blown off in lime set withdrawing can 610, reduces wax condensation postadhesion on upright radiator 620 tube side tube walls, thus the impact that alleviates widely wax heat exchanging effect; Be arranged side by side top structure form at lime set withdrawing can 610 for upright radiator 620 and scum dredger tank 630, non-condensable gas makes progress baffling when leaving separator 600 by scum dredger tank 630 tops outlets, most lime sets fall in the lime set withdrawing can 610 because of gravity, and most of lime set obtains effective separation; And adopt the up and down structure formation of combination for upright radiator in the prior art and lime set withdrawing can, gaseous phase outlet is arranged on the lime set withdrawing can upper portion side wall of upright radiator below, this configuration formula, part lime set and wax just have little time to fall toward contact and have been blown out the lime set withdrawing can by gas phase, it is serious that gas phase is carried drop, and non-condensable gas and drop can not effective separations.Scum dredger tank 630 is used for removing reaction and generates the drop that gas carries.Adopt this separator 600 wax that reaction generates in the gas can be separated, avoided making wax behind downstream unit in traditional paraffin removal method, in case temperature reduces, the wax in the thick methyl alcohol will condense, and has influence on the normal production of downstream unit.In the prior art, upright radiator and lime set withdrawing can adopt the up and down structure formation of combination, and this configuration formula, part lime set and wax just have little time to fall toward contact and blown out the lime set withdrawing can by gas phase, and gas phase is still carried more drop; This upright radiator 620 of the present utility model and scum dredger tank 630 are arranged side by side the structure formation at the top of lime set withdrawing can 610, so that carrying the amount that lime set and wax enter upstream device, gas phase greatly reduces, air-flow is by scum dredger tank 630 scum dredgers, the drop that carries is further removed by scum dredger, and gas phase is carried the lime set amount and further reduced.

Preferably, upright radiator 620 is shell and tube cooler, and the shell side entrance and exit of upright radiator 620 is connected to respectively circulating water pipework and cooling air pipeline, and the upper end of upright radiator 620 is provided with reaction and generates gas entrance 623.Upright radiator 620 shell sides pass into heat-eliminating medium, and heat-eliminating medium is the air of cooling air pipeline or the recirculated water of circulating water pipework.As shown in Figure 1, cooling air inlet mouth 615 and recirculated water water-in 616 are the lower position that the shell side entrance is arranged on described upright radiator 620, and cooling air air outlet 617 and recirculated water water outlet 618 are the upper position that the shell side outlet is arranged on described upright radiator 620.Reaction generates gas entrance 623 and is communicated with the tube side of upright radiator 620, can pass into reaction in the tube side and generate gas.When envrionment temperature is low, adopt air cooled mode to cool off, when the higher cooling air of envrionment temperature can't satisfy cooling when requiring, can close cooling air admission line valve, adjust recirculated water entry pipeline valve opening and adopt the circulating water reaction to generate gas.

Preferably, as shown in figure 11, the bottom of lime set withdrawing can 610 is provided with liquid phase output tube 611, and the inner port that liquid phase output tube 611 stretches in the lime set withdrawing can 610 arrange down, and port is horn-like, and the external port of liquid phase output tube 611 is positioned at outside the lime set tank 610.Horn-like port extends to liquid level below 614, and this trumpet-shaped liquid taking port can avoid causing because of the wax accumulation that is attached near the wax of liquid taking port and falls the problem of liquid taking port obstruction.

Preferably, the bottom of lime set withdrawing can 610 is provided with wax discharging port 613.Lime set withdrawing can bottom is provided with wax discharging port, can pass through the regular de-waxing of wax discharging port.

Preferably, the outer wall of lime set withdrawing can 610 below is provided with well heater 612.When pyroparaffine frozen plug wax discharging port can't de-waxing, the power supply that can connect well heater 612 heated a little to material in the lime set withdrawing can, can continue de-waxing after wax is melted.Preferably, well heater 612 is arranged on the outer wall below of lime set withdrawing can 610 in the form of a ring, is convenient to uniform heating.Further preferably, well heater 612 is electromagnetic heater, electromagnetic heater can be selected heating power according to different operating modes, utilize the characteristics of the strong wide coverage of hertzian wave penetrance, can within the extremely short time, melt the whole waxs that are deposited on lime set withdrawing can bottom, with respect to traditional built-in steam-heated mode, need not to consider condensate drain and the warming problem such as antifreeze, and simple to operate energy-efficient, overhaul very easy to usely, can greatly increase work efficiency.

Preferably, the scum dredger air-flow that scum dredger tank 630 comprises tank body and is arranged on the tank body top is by the scum dredger of scum dredger tank 630, and the drop that carries is further removed by scum dredger, and gas phase is carried the lime set amount and further reduced.

According to the typical embodiment of the utility model, as shown in figure 13, condenser comprises elementary vertical (type) condenser 410, secondary vertical (type) condenser 420 and condenser lime set tank 430, wherein, elementary vertical (type) condenser 410 comprises elementary vertical (type) condenser shell side and is arranged on the interior elementary vertical (type) condenser tube side of elementary vertical (type) condenser shell side; Secondary vertical (type) condenser 420 comprises secondary vertical (type) condenser shell side and is arranged on the interior secondary vertical (type) condenser tube side of secondary vertical (type) condenser shell side, secondary vertical (type) condenser 420 is arranged on the top of elementary vertical (type) condenser, and elementary vertical (type) condenser tube side and secondary vertical (type) condenser tube side are connected, and elementary vertical (type) condenser top is provided with the distance piece that separates for elementary vertical (type) condenser shell side and secondary vertical (type) condenser shell side; Condenser lime set tank 430 is arranged on the bottom of elementary vertical (type) condenser, communicates with elementary vertical (type) condenser tube side.Use the technical solution of the utility model, owing to be provided with primary and secondary condensed in two stages device, and the tube side of condensed in two stages device communicates, condenser condenses liquid holding tank is arranged on the bottom of primary condenser, owing to through condensed in two stages, therefore can generate from reaction and isolate more thick methanol product the gas.And elementary vertical (type) condenser shell side and secondary vertical (type) condenser shell side are spaced apart by distance piece, can use different heat-eliminating mediums, and in the area of water resources shortage, only part makes water as cooling medium, water saving.

Preferably, elementary vertical (type) condenser tube side vertically, be set in parallel in the elementary vertical (type) condenser shell side, and elementary vertical (type) condenser tube side extends downward and forms secondary vertical (type) condenser tube side in the secondary vertical (type) condenser shell side; Be provided with cooling medium inlet tube and cooling medium outlet pipe on elementary vertical (type) condenser shell side and the secondary vertical (type) condenser shell side.Material by tube side can carry out heat exchange through the medium in the two-stage shell side equably like this.

Preferably, cooling medium inlet tube and cooling medium outlet pipe are respectively arranged with flowrate control valve, make things convenient for the cooling medium flow control.

According to the typical embodiment of the utility model, as shown in figure 13, be provided with the first cooling medium inlet tube 411 and the first cooling medium outlet pipe 412 that communicate with elementary vertical (type) condenser shell side on the elementary vertical (type) condenser 410.Be provided with the second cooling medium inlet tube 421, the second cooling medium outlet pipe 422 that communicate with secondary vertical (type) condenser shell side on the secondary vertical (type) condenser 420.Wherein, the cooling medium of elementary vertical (type) condenser 410 can be cooling air or recirculated water.According to the utility model one typical embodiment, the second cooling medium inlet tube 421 is connected with condensation of gas medium inlet pipe 423 and condenses medium inlet pipe 425 away from an end of secondary vertical (type) condenser 420; The second cooling medium outlet pipe 422 is provided with condensation of gas media outlet pipe 424 and condenses media outlet pipe 426 away from an end of secondary vertical (type) condenser 420, i.e. heat-eliminating medium alternatively cooling air or the recirculated water of level vertical (type) condenser 420, condensation of gas media outlet pipe 424 is connected behind variable valve with the first cooling medium outlet pipe 412 again; The first cooling medium inlet tube 411 and the first cooling medium outlet pipe 412 are with elementary vertical (type) condenser 410 geometric centre point symmetries, and the second cooling medium inlet tube 421 and the second cooling medium outlet pipe 422 are with secondary vertical (type) condenser 420 geometric centre point symmetries.When envrionment temperature is low, adopt air cooled mode to cool off, when the higher cooling air of envrionment temperature can't satisfy cooling when requiring, can close the cooling air admission line valve of secondary vertical (type) condenser 420, adjust recirculated water entry pipeline valve opening and adopt the circulating water reaction to generate gas.

Preferably, secondary vertical (type) condenser 420 tops are provided with the circulation gas that communicates with secondary vertical (type) condenser tube side and enter pipe 427, be provided with circulation gas vent pipe 432 on the sidewall of condenser lime set tank 430, be convenient to the material of tube side and the abundant heat exchange of medium in the shell side.Preferably, thick methyl alcohol outlet 433 is arranged on the bottom of condenser lime set tank 430, and conveniently thick methyl alcohol draws.Distance piece is that the parts that can play interval action get final product, and preferably, distance piece is dividing plate 421, and cost is low, and is easy to use.

According to the typical embodiment of the utility model, secondary vertical (type) condenser 420 inner horizontal are provided with a plurality of distance pieces for secondary vertical (type) condenser shell side being divided into separate space, are provided with cooling medium inlet tube and cooling medium outlet pipe on the shell side of a plurality of separate space.Wherein, can pass into different cooling mediums in the space of each separate space, according to actual needs, increase the washability of degree of condensation and medium.

In system for methanol synthesis, because condenser of the present utility model adopts vertical structure, the thick methyl alcohol that condensation is got off falls into condenser lime set tank 430, minimizing circulation gas carries too much methyl alcohol and enters synthesis reactor, (the too high meeting of methanol content causes the growing amount of wax in the building-up process to increase in the reaction gas, and methanol output also can descend thereupon to avoid the generation of too much wax; If maintenance methanol output, just need to strengthen internal circulating load and the cycle index of unreacted synthetic gas, this has increased again energy consumption undoubtedly), the thick methyl alcohol that condensation is got off then is admitted to thick methanol stripper non-condensable gas, residual solution gas and low-boiling-point substance system and removes non-condensable gas, residual solution gas and low-boiling-point substance.In a word, condenser of the present utility model is applied in methanol synthetizing technology and the method, under equal air input, same composition, the equal filling condition of catalyzer and duration of service same period condition, because more thick methanol product in the reactor is removed in condenser, therefore, the wax that produces still less, the methane of generation still less, methanol output is larger.

According to the utility model one typical embodiment, system for methanol synthesis comprises above-mentioned condenser.According to embodiment of the present utility model, fresh synthesis gas enters purified synthesis gas groove 900 through synthetic air compressor 501, purified synthesis gas preheater 802, from purified synthesis gas groove 900 out fresh synthesis gas and from flow through after circulating gas preheater 803 circulation gas out converges into one gas synthesis loop intermediate heat 801 with generate the gas heat exchange from gas solid catalytic reactor 100 reaction out after enter gas solid catalytic reactor 100.Generate gas from gas solid catalytic reactor 100 reaction gas out and enter separator 600 through synthetic loop intermediate heat 801, thick methyl alcohol air cooler 300.Separator 600 circulation gas out enters condenser 400 behind recycle gas compressor 502, condenser 400 out circulating current and converge into one gas from purified synthesis gas groove 900 fresh synthesis gas out and enter gas solid catalytic reactor 100 by synthesis loop intermediate heat 801.Process from entering thick methanol stripper non-condensable gas, residual solution gas and low boilers system after the thick methyl alcohol of condenser 400, separator 600 sub-departments converges.Can send into catalytic cracking system from the wax that separator 600 bottom wax discharging ports 613 are discharged.Enter hydrogen recovery system from separator 600 a small amount of circulation gas out as the venting of speeding, the high-purity hydrogen that obtains after the recovery is incorporated fresh synthesis gas into.

System for methanol synthesis of the present utility model, reactor, condenser, condenser are particularly suitable for the methyl alcohol synthetic reaction process, also can be used for the chemical processes such as methyl ether, methylamine, methyl ether, ammonia synthesis and CO conversion.

To sum up, the utility model flow process itself has the following advantages at least:

1, normally adopts the series-parallel mode of double tower in the prior art, if wherein a tower stops, will cause because circulating and to carry out, react unbalance fast, cause an other tower to stop, and then cause the interlock shutdown of other upstream and downstream devices or the synthetic gas emptying of upstream, cause and greatly lose and waste.And double tower parallel connection technology flow process of the present utility model and system, not only be conducive to reduce facility investment (for example according to an exemplary embodiments of the present utility model, as shown in figure 14, double-reactor can be public the thick methanol separator of a cover, thick methyl alcohol air cooler and synthesis loop intermediate heat, with respect to former DAVY, can save the thick methanol separator of a cover, the investment of thick methyl alcohol air cooler and synthesis loop intermediate heat), be conducive to maintenance, in the situation that a tower stops, can keep the continuity that other devices are produced, avoid the massive losses that stops and cause because of a tower in the prior art.2, adopt system for methanol synthesis of the present utility model, under equal air input, same composition, the equal filling condition of catalyzer and duration of service same period condition, the wax of generation still less, the methane of generation still less, methanol output is larger.

3, adopt system for methanol synthesis of the present utility model, because the use of separator of the present utility model, wax can be separated from thick methanol product, avoided in the prior art wax behind downstream unit, in case temperature reduces, wax in the thick methyl alcohol will condense, and has influence on the normal production of downstream unit.

4, adopt system for methanol synthesis of the present utility model, the simple operations of paraffin removal method is more convenient.

5, adopt system for methanol synthesis of the present utility model, can generate from reaction and isolate more thick methanol product the gas.

6, effectively water saving.

The above is preferred embodiment of the present utility model only, is not limited to the utility model, and for a person skilled in the art, the utility model can have various modifications and variations.All within spirit of the present utility model and principle, any modification of doing, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.

Claims (11)

1. system for methanol synthesis comprises:

Gas solid catalytic reactor (100) is provided with reaction gas entrance and reaction and generates the gas outlet, oiler feed entrance and byproduct steam outlet,

Separator (600) is provided with reaction and generates the gas entrance on the sidewall, the bottom is provided with the liquid phase output tube, and the top is provided with the circulation gas outlet, and described reaction generates the gas entrance and communicates with the reaction generation gas outlet of described gas solid catalytic reactor (100);

It is characterized in that the circulation gas outlet of described separator (600) links to each other with condenser (400), the circulation gas relief outlet of described condenser (400) communicates with the reaction gas entrance of described gas solid catalytic reactor (100).

2. system for methanol synthesis according to claim 1 is characterized in that, also is provided with gas compressor (500) between the circulation gas outlet of described separator (600) and the described condenser (400).

3. system for methanol synthesis according to claim 1, it is characterized in that, described separator (600) is connected with the cooling air pipeline, and described condenser (400) is provided with condensation of gas medium inlet pipe and gas cooling medium outlet pipe, and described system for methanol synthesis further comprises:

Air filter (700) is connected with the cooling air pipeline of described separator (600) and the condensation of gas medium inlet pipe of described condenser (400) respectively by power set (701).

4. system for methanol synthesis according to claim 3, it is characterized in that, described air filter is connected with respectively room air pipeline (702) and ambient air pipeline (703), is respectively arranged with gas flow control valve on described room air pipeline (702) and the described ambient air pipeline (703).

5. system for methanol synthesis according to claim 1 is characterized in that, comprises two the described gas solid catalytic reactors (100) and the described separator (600) that are arranged in parallel.

6. system for methanol synthesis according to claim 1 is characterized in that, described gas solid catalytic reactor (100) comprising:

Reactor shell (101) is formed with the gas inlet pipeline (150) that extends along the sidewall tangential direction on its sidewall;

Beds (110), be arranged in the described reactor shell (101), and form the eddy flow chamber (140) of ring-type between the described reactor shell (101), described beds (110) is hollow circular cylinder, is provided with the through hole (111) that described eddy flow chamber (140) is communicated with described beds (110) inside on the sidewall of described beds (110); And

Heat-exchanger rig is arranged in the described beds (110).

7. system for methanol synthesis according to claim 6 is characterized in that,

Described heat-exchanger rig comprises many heat transfer tubes (130) that are arranged on equably in the described beds (110), wherein, the flow direction of the interior medium of the described heat transfer tube of part (130) is opposite with the flow direction of the interior medium of described heat transfer tube (130) of remainder;

Described system for methanol synthesis also comprises the drum (200) that communicates with described heat transfer tube (130), is provided with variable valve (160) on the back with water inlet line of the described heat transfer tube of part (130) that the water in the described drum (200) enters from bottom to top;

Be provided with thermopair near the inherent described heat transfer tube of described beds (110) (130), the control loop of the flow of described variable valve (160) and the interior water of the described heat transfer tube of described thermopair formation control (130).

8. system for methanol synthesis according to claim 7, it is characterized in that, be provided with on the back with water inlet line of the described heat transfer tube of part (130) that the water in the described drum (200) enters from top to bottom for the variable frequency pump (201) of regulating hydraulic pressure, the exit end of the exit end of the described heat transfer tube of this part (130) and described variable frequency pump (201) is respectively arranged with differential manometer, and described differential manometer and described variable frequency pump (201) form and suppress the control loop that steam flows backwards.

9. system for methanol synthesis according to claim 1 is characterized in that, described separator (600) comprising:

Lime set withdrawing can (610),

Upright radiator (620) is arranged side by side at the top of described lime set withdrawing can (610) with scum dredger tank (630), and all is connected with described lime set withdrawing can (610).

10. system for methanol synthesis according to claim 1 is characterized in that, described condenser (400) comprising:

Elementary vertical (type) condenser (410) comprises elementary vertical (type) condenser shell side and is arranged on the interior elementary vertical (type) condenser tube side of described elementary vertical (type) condenser shell side;

Secondary vertical (type) condenser (420), comprise secondary vertical (type) condenser shell side and be arranged on the interior secondary vertical (type) condenser tube side of described secondary vertical (type) condenser shell side, described secondary vertical (type) condenser (420) is arranged on the top of described elementary vertical (type) condenser, and described elementary vertical (type) condenser tube side and described secondary vertical (type) condenser tube side are connected, and described elementary vertical (type) condenser top is provided with the distance piece that separates for described elementary vertical (type) condenser shell side and described secondary vertical (type) condenser shell side; And

Condenser lime set tank (430) is arranged on the bottom of described elementary vertical (type) condenser, communicates with described elementary vertical (type) condenser tube side.

11. system for methanol synthesis according to claim 2, it is characterized in that, described gas compressor (500) comprises synthesic gas compressor (501) and recycle gas compressor (502), described synthesic gas compressor (501) is provided with the outlet of fresh synthesis gas entrance and fresh synthesis gas, described synthesic gas compressor (501) by syngas outlet successively with purified synthesis gas preheater (802), purified synthesis gas groove (900), synthesis loop intermediate heat (801), described gas solid catalytic reactor (100) is connected; The reaction of described gas solid catalytic reactor (100) generates the gas outlet and is connected with described synthesis loop intermediate heat (801), thick methyl alcohol air cooler (300), described separator (600) successively; The circulation gas outlet of described separator (600) is connected with described recycle gas compressor (502), described condenser (400), circulating gas preheater (803), described synthesis loop intermediate heat (801), described gas solid catalytic reactor (100) successively.

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