CN105038839A - Light dydrocarbon preparation method and light dydrocarbon preparation system with methyl alcohol as raw materials - Google Patents
Light dydrocarbon preparation method and light dydrocarbon preparation system with methyl alcohol as raw materials Download PDFInfo
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Abstract
The invention relates to a light dydrocarbon preparation method with methyl alcohol as raw materials, and further relates to a light dydrocarbon preparation system in which the method is adopted. The method comprises the steps that heat exchange and heating are carried out on the raw materials, methyl alcohol, and discharged materials of a synthesis reactor through an inlet and outlet heat exchanger, and then methyl alcohol and the discharged materials are conveyed into a methyltertiarvbutyl ether reactor; meanwhile, circulating gas is conveyed into the methyltertiarvbutyl ether reactor, the reaction temperature of the methyltertiarvbutyl ether reactor is controlled through the circulating gas conveyed into the methyltertiarvbutyl ether reactor, after heat recycling and cooling, the discharged materials of the synthesis reactor enter a three-phase separation system, and most of a gaseous phase separated out by the three-phase separation system is used as the circulating gas after being boosted by a gas compressor. The preparation system comprises a feed conveying pipeline, the methyltertiarvbutyl ether reactor, the synthesis reactor, the three-phase separation system and an after-separation system capable of separating fuel gas, liquefied gas, light dydrocarbon and heavy oil out of corresponding oil phases. The technological process is simple, control difficulty is low, energy consumption is low, and product quality is high and stable.
Description
Technical field
The present invention relates to a kind of take methyl alcohol as the lighter hydrocarbons preparation method of raw material, also relates to a kind of lighter hydrocarbons preparation system adopting the method.
Background technology
Along with the fast development of global economy and car industry, world petroleum demand amount and automobile fuel consumption constantly rise, and topsoil is on the rise, and public's energy-saving and emission-reduction and environmental consciousness are also in continuous reinforcement.For reply global warming is to the severe challenge of human survival and development, countries in the world automobile exhaust emission standard and fuel oil quality standard are also increasingly strict, Methanol lighter hydrocarbons technology can make crude carbinol directly change into low-sulfur, low alkene, high-octane lighter hydrocarbons, product can direct marketing or be in harmonious proportion mutually with conventional oil refinery gasoline, is met the clean gasoline product of state IV or state V standard.But the device technique flow process of current domestic Methanol lighter hydrocarbons is complicated, material benzenemethanol generally needs to enter reactor after three heating of preheater, vaporizer and superheater, fails fully to reclaim reaction heat, causes energy consumption of unit product high, and its technique controlling difficulty is high, unstable product quality.
Summary of the invention
In order to overcome the above-mentioned defect of prior art, the invention provides a kind of take methyl alcohol as the lighter hydrocarbons preparation method of raw material, additionally provides a kind of lighter hydrocarbons preparation system adopting the method, to simplification of flowsheet, reduce technique controlling difficulty, reduce energy consumption, improve the quality of products.
The technical solution adopted in the present invention:
A kind of take methyl alcohol as the lighter hydrocarbons preparation method of raw material, after material benzenemethanol is heated up by the discharging heat exchange of inlet outlet heat exchanger and synthesis reactor, send into methyltertiarvbutyl ether reactor and carry out etherification reaction, generate dme and water, synthesis reactor is sent in the discharging of methyltertiarvbutyl ether reactor and carries out building-up reactions, generate thick lighter hydrocarbons, while material benzenemethanol is sent into methyltertiarvbutyl ether reactor, circulation gas is also sent into methyltertiarvbutyl ether reactor, the temperature of reaction of methyltertiarvbutyl ether reactor is controlled by the circulation gas sending into methyltertiarvbutyl ether reactor, the discharging of synthesis reactor is entered three-phase separating system after heat recuperation cooling, the gas phase major part that described three-phase separating system is separated uses as circulation gas after gas compressor boosting, on a small quantity can as periodic off-gases, and the separation that rear separation system participates in useful component can be sent into, aqueous phase can be delivered to sewage treatment facility or carry out other process, oil phase is delivered to rear separation system and is separated, isolated product comprises fuel gas, liquefied gas, lighter hydrocarbons and heavy oil.
A kind of take methyl alcohol as the lighter hydrocarbons preparation system of raw material, comprise feed duct road, methyltertiarvbutyl ether reactor, synthesis reactor, three-phase separating system and fuel gas can be gone out from corresponding separation of oil, liquefied gas, the rear separation system of lighter hydrocarbons and heavy oil, described methyltertiarvbutyl ether reactor is connected with described synthesis reactor, the discharging of methyltertiarvbutyl ether reactor enters synthesis reactor, the output channel of described synthesis reactor connects the opening for feed of described three-phase separating system, the gas phase output channel of described three-phase separating system connects the import of gas compressor, the output channel of described gas compressor connects the opening for feed of described methyltertiarvbutyl ether reactor, the output channel of described gas compressor and the mode of connection of the opening for feed of described methyltertiarvbutyl ether reactor are that the output channel of described gas compressor is directly connected with the opening for feed of described methyltertiarvbutyl ether reactor or are that the output channel of described gas compressor accesses described feed duct road, and then be connected with the opening for feed of described methyltertiarvbutyl ether reactor by described feed duct road, the oil phase output channel of described three-phase separating system connects the opening for feed of described rear separation system, the output channel of described synthesis reactor is serially connected with successively the exothermic medium passage of vapour generator and inlet outlet heat exchanger, described vapour generator is provided with the water inlet for accessing deaerated water and the steam output pipe for exporting steam, the heat-absorbing medium passage of described interchanger is serially connected in described feed duct, when the output channel of described gas compressor accesses described feed duct road, access position is preferably placed at the heat-absorbing medium on the suction side of described import and export heat exchanger.
Beneficial effect of the present invention: have effectively achieved the control to methyltertiarvbutyl ether reactor interior reaction temperature by circulation gas, and the control that effectively can realize synthesis reactor interior reaction temperature by circulation gas, and then the control of the reaction depth achieved correlated response and reaction product, particularly effectively can control the component distribution of reaction product and the yield of target product, be conducive to the productive rate improving lighter hydrocarbons, because the heating strength of etherificate and building-up reactions is all higher, it is larger that temperature controls difficulty, and carry out temperature control by the mode sending into circulation gas in import, significantly reduce control difficulty, be conducive to realizing stable and suitable reaction conditions, drastically increase the stability of quality product and quality product, also help the carbon distribution and coking that reduce catalyzer simultaneously, enhance productivity, the regeneration period of extending catalyst and work-ing life, heating material benzenemethanol owing to have employed inlet outlet heat exchanger, can be that the raw material entering methyltertiarvbutyl ether reactor is substantially consistent with temperature of reaction and does not need to consume extra energy, is conducive to carrying out smoothly of reaction, due to vapour generator and inlet outlet heat exchanger are serially connected on the output channel of synthesis reactor successively, thus achieve the abundant of synthetic gas heat energy and effectively utilize, the middle pressure steam that vapour generator produces can be directly used on the steam turbine of gas compression cooperation, be conducive to reducing overall energy consumption, and ensure that the optimal temperature of subsequent technique, on the output channel of methyltertiarvbutyl ether reactor, also can also be connected in series vapour generator simultaneously, not only achieve the effective utilization to reaction Heat of Formation, but also reduce the temperature of charge entering synthesis reactor, be conducive to the optimal temperature keeping synthesis reactor, alleviate the cooling requirement of synthesis reactor.Energy consumption of the present invention is low, is easy to control, and is easy to maintain the stable of processing condition, and production cost is low, and efficiency is high, and good product quality, quality stability is high.
Accompanying drawing explanation
Fig. 1 is the system construction schematic diagram of an embodiment of the present invention;
Fig. 2 is the system construction schematic diagram of the another kind of embodiment of the present invention;
Fig. 3 is the system construction schematic diagram of the third embodiment of the present invention.
Embodiment
The invention provides a kind of take methyl alcohol as the lighter hydrocarbons preparation method of raw material, after material benzenemethanol is heated up by the discharging heat exchange of inlet outlet heat exchanger and synthesis reactor by it, send into methyltertiarvbutyl ether reactor and carry out etherification reaction, generate dme and water, synthesis reactor is sent in the discharging of methyltertiarvbutyl ether reactor and carries out building-up reactions, generate thick lighter hydrocarbons, while material benzenemethanol is sent into methyltertiarvbutyl ether reactor, circulation gas is also sent into methyltertiarvbutyl ether reactor, the temperature of reaction of methyltertiarvbutyl ether reactor is controlled by the circulation gas sending into methyltertiarvbutyl ether reactor, the discharging of synthesis reactor is entered three-phase separating system after heat recuperation cooling, the gas phase major part that described three-phase separating system is separated uses as circulation gas after gas compressor boosting, on a small quantity can as periodic off-gases, and the separation that rear separation system participates in useful component can be sent into, aqueous phase can be delivered to sewage treatment facility or carry out other process, oil phase is delivered to rear separation system and is separated, isolated product comprises fuel gas, liquefied gas, lighter hydrocarbons and heavy oil.
Preferably, the discharging of component loops gas and described methyltertiarvbutyl ether reactor is together sent in synthesis reactor, controlled the temperature of reaction of synthesis reactor by the circulation gas sending into synthesis reactor, and then control the component distribution of building-up reactions product and the yield of target product.
Preferably, the temperature of reaction of described methyltertiarvbutyl ether reactor and synthesis reactor is between 215-430 DEG C, reaction pressure is between 0.3-2.5Mpag, gaseous pressure in described three-phase separating system is between 0.2-2.3Mpag, and the mol ratio of the described circulation gas and methyl alcohol that are used as methyltertiarvbutyl ether reactor charging is between 1-15.
Optionally, the forward slip value of methyltertiarvbutyl ether reactor can entered as the methyl alcohol of methyltertiarvbutyl ether reactor charging and circulation gas, the mixture formed after mixing is sent into methyltertiarvbutyl ether reactor (namely device mixes) outward, also can enter methyltertiarvbutyl ether reactor respectively, realize the mixing (namely mixing in device) in methyltertiarvbutyl ether reactor thus.
Preferably, when as the methyl alcohol of methyltertiarvbutyl ether reactor charging and circulation gas when entering the forward slip value of methyltertiarvbutyl ether reactor, this is blended in before methyl alcohol enters described inlet outlet heat exchanger or in interchanger and carries out, and the mixture be mixed to form carries out heat exchange intensification at inlet outlet heat exchanger.
Optionally, described methyltertiarvbutyl ether reactor and synthesis reactor can be two independent meanss be connected by pipeline, also can be the integrated reactor being provided with etherification reaction section and building-up reactions section, described etherification reaction section and building-up reactions section form described methyltertiarvbutyl ether reactor and described synthesis reactor respectively.
Preferably, when described methyltertiarvbutyl ether reactor and synthesis reactor adopt integrated reactor, described integrated reactor is provided with upper and lower two reaction beds, material sequentially passes through these two beds and carries out required etherification reaction and building-up reactions at two beds respectively, makes these two reaction beds form described etherification reaction section and building-up reactions section respectively thus.
Optionally, be provided with between the etherification reaction section of described integrated reactor and building-up reactions section or be not provided with cold shock pipeline, when being provided with cold shock pipeline between described etherification reaction section and building-up reactions section, circulation gas is sent in described cold shock pipeline as cold shock gas, to be controlled the temperature of building-up reactions section by cold shock mode.
Optionally, adopt any one or a few mode following to carry out energy recovery that reactor (methyltertiarvbutyl ether reactor and/or synthesis reactor) reacts Heat of Formation: (1) arranges heat transfer tube in the reactor, in heat transfer tube, pass into cold medium flow carry out absorb heat (i.e. heat-obtaining in device), reduce while reclaiming heat energy or control the temperature in synthesis reactor; (2) intermediate material not completing total overall reaction is drawn reactor, heat exchange is carried out by heat exchanger and cold medium flow, return after cooling in this reactor and proceed to react (i.e. device outside heat removing), reduce while reclaiming heat energy or control the temperature in synthesis reactor; (3) discharging of reactor introducing heat exchanging apparatus and cold medium flow are carried out heat exchange, after cooling, enter next operation.
Preferably, the output channel of described synthesis reactor is in series with vapour generator and described inlet outlet heat exchanger, before described vapour generator is positioned at described inlet outlet heat exchanger, the discharging of described synthesis reactor first through the exothermic medium of vapour generator as vapour generator, and then is heated through the mixture of inlet outlet heat exchanger to methyl alcohol or methyl alcohol and circulation gas.
Preferably, described vapour generator is middle pressure steam producer, the middle pressure steam driving steam turbine work generated with vapour generator.
Optionally, described three-phase separating system mainly comprises the three phase separation tank that can realize gas, water, oily three phase separation, also a knockout drum and a gun barrel can mainly be comprised, realize being separated of gas phase and liquid phase by knockout drum, the liquid phase after being separated is sent into water-and-oil separator and realize being separated of aqueous phase and oil phase.
Optionally, gas phase boosting for being separated by three-phase separating system can for independent gas compressor as the compressor of circulation gas, it can be the compressor in compressor and the two-in-one unit of steam turbine, it can be the compressor in the three-in-one unit of compressor, steam turbine and electric motor, it can also be the compressor in compressor, steam turbine, generator and electric motor four-in-one unit, when being in series with middle pressure steam producer on the output channel of described synthesis reactor, the middle pressure steam that described middle pressure steam producer produces can be used as the power of described steam turbine.
See Fig. 1-3, present invention also offers a kind of take methyl alcohol as the lighter hydrocarbons preparation system of raw material, this system can adopt any one method above-mentioned to prepare light body, it comprises feed duct road 81, methyltertiarvbutyl ether reactor 10, synthesis reactor 20, three-phase separating system and fuel gas can be gone out from corresponding separation of oil, liquefied gas, the rear separation system 50 of lighter hydrocarbons and heavy oil, described methyltertiarvbutyl ether reactor is connected with described synthesis reactor, the discharging of methyltertiarvbutyl ether reactor enters synthesis reactor, the output channel 21 of described synthesis reactor connects the opening for feed of described three-phase separating system, the gas phase output channel 43 of described three-phase separating system connects the import of gas compressor 60, the output channel 61 of described gas compressor connects the opening for feed of described methyltertiarvbutyl ether reactor, the output channel of described gas compressor and the mode of connection of the opening for feed of described methyltertiarvbutyl ether reactor are that the output channel of described gas compressor is directly connected with the opening for feed of described methyltertiarvbutyl ether reactor or are that the output channel of described gas compressor accesses described feed duct road, and then be connected with the opening for feed of described methyltertiarvbutyl ether reactor by described feed duct road, the oil phase output channel 41 of described three-phase separating system connects the opening for feed of described rear separation system, the output channel of described synthesis reactor is serially connected with successively the exothermic medium passage of vapour generator 30 and inlet outlet heat exchanger 70, described vapour generator is provided with the water inlet 32 for accessing deaerated water and the steam output pipe 31 for exporting steam, the heat-absorbing medium passage of described interchanger is serially connected in described feed duct, when the output channel of described gas compressor accesses described feed duct road, access position is preferably placed at the heat-absorbing medium on the suction side of described import and export heat exchanger.
Preferably, the gas phase output channel of described three-phase separating system is divided into two-way, the end on one tunnel 44 is connected in the import of described gas compressor, realize the connection of the gas phase output channel of described three-phase separating system and the import of described gas compressor thus, the periodic off-gases import of described rear separation system, as periodic off-gases transport pipe, is accessed in another road 45.
Optionally, the aqueous phase output channel 42 of described three-phase separating system accesses waste disposal plant.
Optionally, described three-phase separating system mainly comprises the three phase separation tank 40 that can realize gas, water, oily three phase separation, also a knockout drum 40.2 and a gun barrel 40.1 can mainly be comprised, realize being separated of gas phase and liquid phase by knockout drum, the liquid phase after being separated is sent into water-and-oil separator and realize being separated of aqueous phase and oil phase.
Preferably, the output channel of described gas compressor is provided with circulation gas cold shock pipeline 62, and described circulation gas cold shock pipeline accesses the import of described synthesis reactor or accesses the output channel 11 of described methyltertiarvbutyl ether reactor.
Preferably, the output channel of described methyltertiarvbutyl ether reactor is also serially connected with vapour generator 90, to realize energy recovery and to avoid the temperature of synthesis reactor described in lifting.
Preferably, the steam vapour generator that the vapour generator that the output channel of described synthesis reactor is connected in series and/or the output channel of described methyltertiarvbutyl ether reactor are connected in series is middle pressure steam producer.
Optionally, described methyltertiarvbutyl ether reactor and synthesis reactor can be two independent meanss be connected by pipeline, also can be the integrated reactor being provided with etherification reaction section and building-up reactions section, described etherification reaction section and building-up reactions section form described methyltertiarvbutyl ether reactor and described synthesis reactor respectively.
Preferably, when described methyltertiarvbutyl ether reactor and synthesis reactor adopt integrated reactor, described integrated reactor is provided with upper and lower two reaction beds 10.1,10.2, material sequentially passes through these two beds and carries out required etherification reaction and building-up reactions at two beds respectively, makes these two reaction beds form described etherification reaction section and building-up reactions section respectively thus.
Optionally, be provided with between the etherification reaction section of described integrated reactor and building-up reactions section or be not provided with cold shock pipeline, when being provided with cold shock pipeline between described etherification reaction section and building-up reactions section, circulation gas is sent in described cold shock pipeline as cold shock gas, to be controlled the temperature of building-up reactions section by cold shock mode.
Preferably, described gas compressor is provided with steam turbine, when the steam vapour generator be connected in series on the output channel of the vapour generator that the output channel stating synthesis reactor is connected in series and/or described methyltertiarvbutyl ether reactor is middle pressure steam producer, the steam output pipe of described middle pressure steam producer accesses the steam inlet of described steam turbine.
Here is several specific embodiment of the present invention:
Embodiment 1(such as Fig. 1 shows):
Form parallel feeding after material benzenemethanol and circulation gas mixing, after inlet outlet heat exchanger and synthesis reactor discharging heat exchange heat up, enter methyltertiarvbutyl ether reactor successively and synthesis reactor generates thick lighter hydrocarbons.Circulation gas cold shock pipeline (dotted line represents) can be set between methyltertiarvbutyl ether reactor and synthesis reactor.Middle pressure steam producer byproduct steam is first delivered in synthesis reactor discharging, then through inlet outlet heat exchanger heating parallel feeding, further heat recuperation, enters three phase separation tank finally by after cooling (as air-cooler, water cooler cooling).Isolated gas phase major part is back to reactor as reaction cycle gas after compressor boosting, speeds on a small quantity to put; Aqueous phase delivers to sewage treatment facility; Oil phase delivers to rear separation system.
Control the molar flow of reaction cycle gas and material benzenemethanol than being 5-8; The temperature in controlling methyltertiarvbutyl ether reactor is 290 DEG C, and etherification reaction pressure is 1.9Mpag; Controlling three-phase separating system gaseous pressure is 1.47Mpag.
Embodiment 2(such as Fig. 2 shows):
Form parallel feeding after material benzenemethanol and circulation gas mixing, after inlet outlet heat exchanger and synthesis reactor discharging heat exchange heat up, enter methyltertiarvbutyl ether reactor and react.Methyltertiarvbutyl ether reactor discharging enters synthesis reactor and proceeds reaction after delivering to middle pressure steam producer byproduct steam.Middle pressure steam producer byproduct steam is delivered in conversion zone discharging, then through the further heat recuperation of parallel feeding interchanger, enters three phase separation tank finally by after cooling (as air-cooler, water cooler cooling).Isolated gas phase major part is back to reactor as reaction cycle gas after compressor boosting, speeds on a small quantity to put; Aqueous phase delivers to sewage treatment facility; Oil phase delivers to rear separation system.
Control the molar flow of reaction cycle gas and material benzenemethanol than being 2-5; The temperature in controlling methyltertiarvbutyl ether reactor is 300 DEG C, and etherification reaction pressure is 1.95Mpag; Controlling three-phase separating system gaseous pressure is 1.46Mpag.
Embodiment 3(such as Fig. 3 shows):
Form parallel feeding after material benzenemethanol and circulation gas mixing, after inlet outlet heat exchanger and synthesis reactor discharging heat exchange heat up, enter integrated reactor and generate thick lighter hydrocarbons.Integrated reactor is divided into etherificate section and upper and lower two reaction beds of synthesis stage, can arrange reaction cycle air cooling and swash pipeline (dotted line represents) between bed.Middle pressure steam producer byproduct steam is first delivered in the discharging of building-up reactions section, then through the further heat recuperation of parallel feeding interchanger, enters three-phase separating system finally by after cooling (as air-cooler, water cooler cooling).Three-phase separating system can be the triphase separator of a band water bag, or a gas-liquid separator and a water-and-oil separator combine (dotted line represents).Isolated gas phase major part is back to reactor as reaction cycle gas after compressor boosting, speeds on a small quantity to put; Aqueous phase delivers to sewage treatment facility; Oil phase delivers to rear separation system.
Control the molar flow of reaction cycle gas and material benzenemethanol than being 5-8; The temperature in controlling methyltertiarvbutyl ether reactor is 300 DEG C, and etherification reaction pressure is 1.9Mpag; Controlling three-phase separating system gaseous pressure is 1.45Mpag.
Each preferred and optional technique means disclosed by the invention, unless otherwise indicated and one preferably or alternatives means be outside the further restriction of another technique means, all can arbitrary combination, form some different technical schemes.
Claims (10)
1. one kind take methyl alcohol as the lighter hydrocarbons preparation method of raw material, after material benzenemethanol is heated up by the discharging heat exchange of inlet outlet heat exchanger and synthesis reactor, send into methyltertiarvbutyl ether reactor and carry out etherification reaction, generate dme and water, synthesis reactor is sent in the discharging of methyltertiarvbutyl ether reactor and carries out building-up reactions, generate thick lighter hydrocarbons, it is characterized in that, while material benzenemethanol is sent into methyltertiarvbutyl ether reactor, circulation gas is also sent into methyltertiarvbutyl ether reactor, the temperature of reaction of methyltertiarvbutyl ether reactor is controlled by the circulation gas sending into methyltertiarvbutyl ether reactor, the discharging of synthesis reactor is entered three-phase separating system after heat recuperation cooling, the gas phase major part that described three-phase separating system is separated uses as circulation gas after gas compressor boosting, oil phase is delivered to rear separation system and is separated, isolated product comprises fuel gas, liquefied gas, lighter hydrocarbons and heavy oil.
2. preparation method as claimed in claim 1, the discharging of component loops gas and described methyltertiarvbutyl ether reactor is it is characterized in that together to send in synthesis reactor, controlled the temperature of reaction of synthesis reactor by the circulation gas sending into synthesis reactor, and then control the component distribution of building-up reactions product and the yield of target product.
3. preparation method as claimed in claim 3, it is characterized in that the temperature of reaction of described methyltertiarvbutyl ether reactor and synthesis reactor is between 215-430 DEG C, reaction pressure is between 0.3-2.5Mpag, gaseous pressure in described three-phase separating system is between 0.2-2.3Mpag, and the mol ratio of the described circulation gas and methyl alcohol that are used as methyltertiarvbutyl ether reactor charging is between 1-15.
4. as claim 1, preparation method described in 2 or 3, it is characterized in that entering the forward slip value of methyltertiarvbutyl ether reactor as the methyl alcohol of methyltertiarvbutyl ether reactor charging and circulation gas, the mixture formed after mixing is sent into methyltertiarvbutyl ether reactor, or enter methyltertiarvbutyl ether reactor respectively as the methyl alcohol of methyltertiarvbutyl ether reactor charging and circulation gas, when as the methyl alcohol of methyltertiarvbutyl ether reactor charging and circulation gas when entering the forward slip value of methyltertiarvbutyl ether reactor, this is blended in before methyl alcohol enters described inlet outlet heat exchanger or in interchanger and carries out, the mixture be mixed to form carries out heat exchange intensification at inlet outlet heat exchanger.
5. as claim 1, preparation method described in 2 or 3, it is characterized in that described methyltertiarvbutyl ether reactor and synthesis reactor are two independent meanss be connected by pipeline, or be provided with the integrated reactor of etherification reaction section and building-up reactions section, described etherification reaction section and building-up reactions section form described methyltertiarvbutyl ether reactor and described synthesis reactor respectively, when described methyltertiarvbutyl ether reactor and synthesis reactor adopt integrated reactor, described integrated reactor is provided with, lower two reaction beds, material sequentially passes through these two beds and carries out required etherification reaction and building-up reactions at two beds respectively, these two reaction beds form described etherification reaction section and building-up reactions section respectively, be provided with between the etherification reaction section of described integrated reactor and building-up reactions section or be not provided with cold shock pipeline, when being provided with cold shock pipeline between described etherification reaction section and building-up reactions section, circulation gas is sent in described cold shock pipeline as cold shock gas, to be controlled the temperature of building-up reactions section by cold shock mode.
6. the preparation method as described in claim 1,2 or 3, it is characterized in that adopting any one or a few mode following to carry out the energy recovery of reactor reaction Heat of Formation: (1) arranges heat transfer tube in the reactor, in heat transfer tube, pass into cold medium flow absorb heat, reduce while reclaiming heat energy or control the temperature in synthesis reactor; (2) intermediate material not completing total overall reaction is drawn reactor, carry out heat exchange by heat exchanger and cold medium flow, return after cooling in this reactor and proceed reaction, reduce while reclaiming heat energy or control the temperature in synthesis reactor; (3) discharging of reactor introducing heat exchanging apparatus and cold medium flow are carried out heat exchange, after cooling, enter next operation.
7. the preparation method as described in claim 1,2 or 3, the output channel that it is characterized in that described synthesis reactor is in series with vapour generator and described inlet outlet heat exchanger, before described vapour generator is positioned at described inlet outlet heat exchanger, the discharging of described synthesis reactor first through the exothermic medium of vapour generator as vapour generator, and then is heated through the mixture of inlet outlet heat exchanger to methyl alcohol or methyl alcohol and circulation gas.
8. the preparation method as described in claim 1,2 or 3, it is characterized in that described three-phase separating system mainly comprises the three phase separation tank that can realize gas, water, oily three phase separation, or mainly comprise a knockout drum and a gun barrel, realize being separated of gas phase and liquid phase by knockout drum, the liquid phase after being separated is sent into water-and-oil separator and realize being separated of aqueous phase and oil phase.
9. one kind take methyl alcohol as the lighter hydrocarbons preparation system of raw material, comprise feed duct road, methyltertiarvbutyl ether reactor, synthesis reactor, three-phase separating system and fuel gas can be gone out from corresponding separation of oil, liquefied gas, the rear separation system of lighter hydrocarbons and heavy oil, described methyltertiarvbutyl ether reactor is connected with described synthesis reactor, the discharging of methyltertiarvbutyl ether reactor enters synthesis reactor, the output channel of described synthesis reactor connects the opening for feed of described three-phase separating system, the gas phase output channel of described three-phase separating system connects the import of gas compressor, the output channel of described gas compressor connects the opening for feed of described methyltertiarvbutyl ether reactor, the output channel of described gas compressor and the mode of connection of the opening for feed of described methyltertiarvbutyl ether reactor are that the output channel of described gas compressor is directly connected with the opening for feed of described methyltertiarvbutyl ether reactor or are that the output channel of described gas compressor accesses described feed duct road, and then be connected with the opening for feed of described methyltertiarvbutyl ether reactor by described feed duct road, the oil phase output channel of described three-phase separating system connects the opening for feed of described rear separation system, the output channel of described synthesis reactor is serially connected with successively the exothermic medium passage of vapour generator and inlet outlet heat exchanger, described vapour generator is provided with the water inlet for accessing deaerated water and the steam output pipe for exporting steam, the heat-absorbing medium passage of described interchanger is serially connected in described feed duct, when the output channel of described gas compressor accesses described feed duct road, access position is preferably placed at the heat-absorbing medium on the suction side of described import and export heat exchanger.
10. preparation method as claimed in claim 9, it is characterized in that the gas phase output channel of described three-phase separating system is divided into two-way, the end on one tunnel is connected in the import of described gas compressor, realize the connection of the gas phase output channel of described three-phase separating system and the import of described gas compressor thus, another road is as periodic off-gases transport pipe, access the periodic off-gases import of described rear separation system, the output channel of described gas compressor is provided with circulation gas cold shock pipeline, described circulation gas cold shock pipeline accesses the import of described synthesis reactor or accesses the output channel of described methyltertiarvbutyl ether reactor, the output channel of described methyltertiarvbutyl ether reactor and/or synthesis reactor is serially connected with vapour generator.
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| CN110791307A (en) * | 2019-12-03 | 2020-02-14 | 新榕能源(福建)有限公司 | Energy-saving temperature control heat exchange system for methanol-to-oil |
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