CN209772061U - Normal-temperature feeding reaction hydrocarbon preparation equipment based on methanol - Google Patents

Abstract

the utility model discloses a hydrocarbon preparation equipment based on methanol normal atmospheric temperature feeding reaction. The device adopts low-temperature direct feeding or atomization feeding and consists of a raw material tank, a tubular reactor, a condenser, a hydrocarbon product tank, a gas-liquid separator and a communicating pipeline, wherein the raw material in the raw material tank at least comprises methanol; the shell and tube reactor comprises a barrel, a constant temperature tube assembly positioned in the barrel, a feed inlet arranged on the side wall of the barrel and a discharge outlet arranged at the bottom of the barrel; the constant temperature tube assembly comprises a plurality of constant temperature tubes, tube plates and a catalyst fixer; the tube plate is fixed on the side wall of the cylinder body, and the constant temperature tube is fixed on the tube plate; the raw material tank is communicated with the tube type reactor through a communicating pipeline; the condenser is positioned between the tubular reactor and the gas-liquid separator. The utility model has the advantages of energy saving, equipment and high conversion rate.

Description

Normal-temperature feeding reaction hydrocarbon preparation equipment based on methanol

Technical Field

The utility model relates to a chemical industry equipment and chemical industry process flow field, more specifically says that it is based on methyl alcohol normal atmospheric temperature feeding reaction hydrocarbon preparation equipment.

Background

Existing reactors include fixed bed reactors, fluidized bed reactors, and multi-tubular reactors. The disadvantages of the fixed bed reactor in use are: the discharged heat cannot be well moved out of the reactor to generate temperature runaway, and the temperature control needs to be carried out by using circulating gas which is 7 times or more than that of the fed methanol, so that the stability of a reaction product and the service life of the catalyst are seriously influenced, the regeneration period of the catalyst is shortened, and the process and equipment are complex, high in energy consumption and high in investment; the disadvantages of the fluidized bed reactor in use are: the catalyst carried in the reaction product needs to be separated, so that the investment cost of equipment is increased; because the catalyst in the fluidized bed moves, the catalyst can be broken, the powdered catalyst is not easy to be separated from reaction products, and the catalyst loss can be increased; the disadvantages of the multitubular reactor in use are: the method adopts a common pipe, because of strong exothermic reaction, the temperature difference between a pipe side and a shell side is too large, and only materials with large specific heat capacity can be used for removing heat, but the heat cannot meet the requirement of raw material heating of continuous feeding after being removed; if the removed heat is less, the bed layer can influence the catalyst due to over-temperature, and the equipment cost can be greatly increased only by increasing the number of heat exchange tubes; the multitubular reactor will not completely regenerate the catalyst because there is no gas distributor at the feed. None of these three reactors alone completely satisfy the relatively efficient use of catalyst in the reactor.

Existing hydrocarbon production facilities: the operating pressure of the feeding port is more than 2.2MPa, the feeding temperature is high (more than 300 ℃), and the reactor can be fed when the reaction temperature is reached; the fixed bed circulation ratio is more than 7:1, various reactors are arranged in the process of exothermic reaction to ensure the reaction conditions and the performances of different catalysts, and the process is complex; the requirement on the volume of equipment is large, and large-scale industrial production is not convenient to realize; large equipment investment, high production cost and low yield of the product oil.

The existing application numbers are: CN201510142484, patent name: a moving bed methanol-to-hydrocarbon method is disclosed, wherein the raw material is gasified at high temperature and then fed, the feeding amount of the gasified raw material is not easy to control, and the operation is unstable.

It is prejudicial to those skilled in the art that the feedstock can only enter the reactor at elevated temperature and pressure to react to produce hydrocarbons.

Therefore, there is a need for a reaction hydrocarbon production facility that saves energy and equipment and has a high conversion rate.

Disclosure of Invention

The utility model aims at providing a hydrocarbon preparation equipment based on methanol normal temperature feeding reaction, the adopted tubular reactor can effectively remove the redundant heat in the reaction tube, simultaneously, the raw material is heated to the required reaction temperature by utilizing the heat in the reactor, the circulation ratio is lower, the energy and the equipment are saved, the conversion rate is higher, the products produced by the equipment are diversified, and a plurality of mixed raw materials containing methanol can be converted simultaneously; the method takes methanol as a heat source, adopts low-temperature direct feeding or atomized feeding at the temperature lower than 100 ℃, utilizes circulating gas to drive, adopts atomization and other means to atomize the feeding when the feeding enters a reactor, controls the temperature of a bed layer of the reactor, and directionally recovers products.

In order to realize the purpose, the technical scheme of the utility model is that: hydrocarbon preparation equipment based on methanol normal temperature feeding reaction, which is characterized in that: adopting low-temperature direct feeding or atomized feeding below 100 ℃, wherein the low-temperature direct feeding or atomized feeding comprises a raw material tank, a tubular reactor, a condenser, a hydrocarbon product tank, a gas-liquid separator and a communicating pipeline; the shell and tube reactor comprises a barrel, a constant temperature tube assembly positioned in the barrel, a feed inlet arranged on the side wall of the barrel and a discharge outlet arranged at the bottom of the barrel; the raw material tank is communicated with the shell and tube reactor through a communicating pipeline, the condenser is located between the shell and tube reactor and the gas-liquid separator, two ends of the condenser are communicated with the discharge port and the gas-liquid separator through the communicating pipeline respectively, the liquid discharge port at the lower end of the gas-liquid separator is communicated with the hydrocarbon product tank through the communicating pipeline, and the gas discharge port at the upper end of the gas-liquid separator is communicated with the feed port through the communicating pipeline.

in the technical scheme, the two transverse ends of the tube plate are respectively fixed on the inner side wall of the cylinder; the two tube plates are respectively a first tube plate fixed at the upper part of the cylinder and a second tube plate fixed at the lower part of the cylinder; the upper end of the constant temperature tube is fixed on the first tube plate and extends upwards out of the first tube plate, and the lower end of the constant temperature tube is fixed on the second tube plate and extends downwards out of the second tube plate; the catalyst fixer is respectively positioned at the upper end and the lower end of the constant temperature pipe; the feed inlet is located between the first tube plate and the second tube plate.

In the technical scheme, the constant temperature pipe is at least one of a light pipe, a finned pipe, a corrugated pipe and a trapezoid pipe, and a catalyst is positioned in the constant temperature pipe.

In the technical scheme, the raw material in the raw material tank is a mixture which takes methanol as a basic raw material and is matched with hydrocarbon and/or carbon oxide and/or carbon monoxide and/or carbon dioxide and/or natural gas.

In the technical scheme, one or more feed inlets are arranged, and when the number of the feed inlets is multiple, the feed inlets are arranged in a circumferential and/or vertical manner; the constant temperature tube assembly comprises a plurality of constant temperature tubes, tube plates and a catalyst fixer; the tube plate is fixed on the side wall of the cylinder body, and the constant temperature tube is fixed on the tube plate; the constant temperature tube assemblies positioned in the tubular reactor have one or more groups.

In the technical scheme, a circulating channel inlet is formed in the upper end of the cylinder, a circulating channel outlet is formed in the side wall of the cylinder, the circulating channel outlet is formed between the first tube plate and the second tube plate and located in the upper portion of the side wall of the cylinder, and the circulating channel outlet is communicated with the circulating channel inlet through a communicating pipeline.

In the above technical scheme, a gas lift pipe is arranged in the barrel, the gas lift pipe is located between two adjacent constant temperature pipes, the gas lift pipe is fixed on the first pipe plate, the upper end of the gas lift pipe extends upwards out of the first pipe plate, the lower end of the gas lift pipe is located between the first pipe plate and the second pipe plate, and the distance between the lower end of the gas lift pipe and the second pipe plate is adjustable.

In the technical scheme, the number of the air lifting pipes is multiple, and the air lifting pipes are light pipes or finned pipes.

In the technical scheme, the catalyst is suitable for methanol reaction and is at least one or more of ZSM-5, MTO-100, MAPSO molecular sieve and ELPSO molecular sieve.

In the above technical solution, the tubular reactor is at least provided with a group of constant temperature tube assemblies, the tubular reactor can be a combined reactor, and has a plurality of combination modes, at least one of a plurality of groups of constant temperature tube assemblies, a group of constant temperature tube assemblies and a group of fixed beds, a plurality of groups of constant temperature tube assemblies and a group of fixed beds, a group of constant temperature tube assemblies and a group of fixed beds, and a group of constant temperature tube assemblies and a plurality of groups of fixed beds.

The utility model discloses a low temperature direct feed or atomizing feeding principle is: the methanol is liquid, can react only when the reaction temperature is reached, the methanol is fed in a liquid form, so that the steps and equipment such as preheating, gasification and the like are omitted, more heat can be consumed, the circulation ratio is reduced, more heat can be removed, and the reaction temperature gradient can be controlled conveniently;

The utility model has high conversion rate because the device effectively controls the reaction temperature to maximize the activity of the catalyst, which is beneficial to the reaction, and the light components and the recycle gas generated at the same time continuously participate in the reaction to generate effective substances, which is also the reason of high conversion rate; if unqualified products are generated, the unqualified products are pumped back through the circulating gas conveying pipeline to be used as reactants to continue reacting in the reactor, and the reaction is repeatedly carried out in such a way, so that the conversion rate can reach a higher level.

The utility model has the advantages of as follows:

(1) The raw materials of the utility model are directly fed or atomized and fed at low temperature lower than 100 ℃ without a preheater, an evaporator and a superheater, and methanol is used as a heat source to prepare hydrocarbon, so that the raw materials containing methanol can be efficiently converted, and the conversion rate reaches 98 percent and above; the technical prejudice that the raw materials in the prior art can be reacted to prepare hydrocarbon only after being gasified at high temperature and high pressure in a reactor is overcome;

(2) The utility model saves energy and equipment, adopts low temperature lower than 100 ℃ to directly feed or atomize and feed, takes away a large amount of reaction heat, more effectively controls the temperature of a reaction bed layer, obtains a required bed layer temperature gradient, and ensures the stable temperature of the bed layer; the utility model adopts the low temperature of less than 100 ℃ for direct feeding or atomized feeding, which is convenient for controlling the feeding amount of raw materials and has stable operation; the defects that the raw materials are fed after being gasified at high temperature, the feeding amount of the gasified raw materials is not easy to control, and the operation is unstable in the prior art are overcome; the conversion rate of the utility model is 98 percent and above;

(3) The reaction circulation ratio of the utility model is below 1:1, the utility model can directionally recover the required products by controlling the temperature of the reactor bed layer and feeding, and the converted products are diversified; the utility model discloses a tubular reactor can simultaneously convert a plurality of mixed raw materials containing methanol; the heat discharged from the discharge port of the tubular reactor can be used for other purposes, and the heat carried by the reaction product can be used for producing steam or generating electricity without loss;

(4) The utility model can convert a plurality of raw materials containing methanol, and the raw materials which can be converted by the utility model are hydrocarbon which is mixed with waste mineral oil, liquefied gas and heavy alkyne and carbon oxide which comprises carbon monoxide and carbon dioxide on the basis of methanol;

(5) The utility model adopts gas, liquid and solid three-phase reaction, and controls the bed temperature of the reactor to directionally obtain the required product through low-temperature direct feeding or atomized feeding and the reaction of the catalyst in the thermostatic tube; the method overcomes the defects that the feeding temperature needs to be raised (more than 300 ℃) to reach the reaction temperature and the reactor can only be fed with the gas-solid two-phase reaction in the prior art, the required equipment is more, and the energy loss is larger.

The device and the method of the utility model are suitable for all exothermic reactions (such as hydrocarbon production reaction, alcohol production reaction, etc.) which need temperature control; the removal of heat in the exothermic reaction and the control of the reaction temperature gradient are the key points for ensuring the product conversion rate and the service life of the catalyst; the device and the method can shift out heat in the exothermic reaction, control the reaction temperature gradient, and ensure the conversion rate of the product and the service life of the catalyst. In the prior art, the heat in the exothermic reaction is controlled by methods of controlling the size of the circulation ratio and/or feeding in a segmented and multistage manner and/or removing the heat by using a split-tube shell filled with heat-conducting liquid, but the radial and longitudinal temperature difference is easy to occur due to the large circulation ratio, so that the reaction is uneven, the volume of equipment is increased, and the investment cost of the equipment is increased; the multistage feeding affects the continuity of the reaction and the operation is unstable; the conversion rate of the heat transferred by the cracked tube heat-conducting liquid is low, the control range of the temperature gradient is limited, and the reaction in the reactor is not facilitated.

Drawings

FIG. 1 is a schematic structural view of the thermostatic tube of the present invention, which is a light tube, and a circulating channel is arranged on the top of the tubular reactor.

FIG. 2 is a schematic structural view of the utility model of a structure with a finned tube and a circulating channel on the top of a tubular reactor.

FIG. 3 is a schematic view of the structure of the constant temperature tube of the present invention, which is a light tube, and a gas lift tube is arranged in the tube-type reactor.

fig. 4 is a schematic structural view of the thermostatic tube of the present invention, in which the light tube, the barrel body are provided with the gas rising tube, a set of thermostatic tube assemblies and a set of fixed bed.

Fig. 5 is a schematic structural view of the thermostatic tube of the present invention, which is a light tube, a gas-raising tube arranged in the barrel, and two groups of thermostatic tube assemblies arranged at intervals.

Fig. 6 is a schematic structural view of the thermostatic tube of the present invention being a light tube, having a plurality of feed inlets, and having a gas-raising tube disposed in the barrel.

Fig. 7 is a schematic structural view of the thermostatic tube of the present invention being a corrugated tube and a gas-raising tube arranged in the tube body.

Fig. 8 is a schematic structural view of the constant temperature tube of the present invention being a wave coil tube and a gas lift tube arranged in the barrel.

Fig. 9 is a schematic structural view of the thermostatic tube of the present invention being a trapezoidal tube and a gas-raising tube being provided in the barrel.

In the figure, 1-raw material tank, 2-tubular reactor, 2.1-constant temperature tube, 2.11-catalyst, 2.2-tube plate, 2.21-first tube plate, 2.22-second tube plate, 2.3-catalyst fixer, 2.4-feed inlet, 2.5-discharge outlet, 2.6-cylinder, 2.7-circulating channel inlet, 2.8-circulating channel outlet, 2.9-riser, 2.10-fixed bed, 2.12-constant temperature tube component, 3-condenser, 3.1-circulating condensed water system, 4-hydrocarbon product tank, 5-gas-liquid separator, 5.1-liquid discharge outlet, 5.2-gas discharge outlet and 6-circulating gas.

Detailed Description

the following detailed description of the embodiments of the present invention will be made with reference to the accompanying drawings, which are not intended to limit the present invention, but are merely exemplary. While the advantages of the invention will be clear and readily appreciated by the description.

With reference to the accompanying drawings: the hydrocarbon preparation equipment based on methanol normal-temperature feeding reaction adopts low-temperature direct feeding or atomization feeding below 100 ℃, and comprises a raw material tank 1, a tubular reactor 2, a condenser 3, a hydrocarbon product tank 4, a gas-liquid separator 5 and a communicating pipeline, wherein the raw material in the raw material tank 1 at least comprises methanol, the methanol is a strong exothermic reaction raw material, and when the raw material is introduced into the tubular reactor 2 at normal temperature for reaction, the raw material methanol is used as a heat source for hydrocarbon preparation reaction; the device comprises a shell 2.6 of the tubular reactor 2, a constant temperature tube assembly 2.12 positioned in the shell 2.6, a feed inlet 2.4 arranged on the side wall of the shell 2.6 and a discharge outlet 2.5 arranged at the bottom of the shell 2.6; raw material tank 1 through the intercommunication pipeline with the feed inlet 2.4 intercommunication of shell and tube reactor 2, condenser 3 is located shell and tube reactor 2 with between the vapour and liquid separator 5, 3 both ends of condenser respectively through the intercommunication pipeline with discharge gate 2.5 with vapour and liquid separator 5 intercommunication, be located liquid discharge gate 5.1 of vapour and liquid separator 5 lower extreme lets in through the intercommunication pipeline hydrocarbon product jar 4, be located gas discharge gate 5.2 of vapour and liquid separator 5 upper end lets in through the intercommunication pipeline feed inlet 2.4, the raw materials is not through preheater, evaporimeter and over heater, directly adopts the normal atmospheric temperature feeding, uses methyl alcohol as the heat source system hydrocarbon, can control reactor bed temperature, the high-efficient raw materials that contains methyl alcohol that converts.

The two transverse ends of the tube plate 2.2 are respectively fixed on the inner side wall of the cylinder 2.6; the number of the tube plates 2.2 is two, namely a first tube plate 2.21 fixed at the upper part of the cylinder 2.6 and a second tube plate 2.22 fixed at the lower part of the cylinder 2.6; the upper end of the constant temperature tube 2.1 is fixed on the first tube plate 2.21 and extends upwards out of the first tube plate 2.21, and the lower end of the constant temperature tube is fixed on the second tube plate 2.22 and extends downwards out of the second tube plate 2.22, so that the constant temperature tube can be fixed up and down conveniently; the catalyst fixer 2.3 is respectively positioned at the upper end and the lower end of the constant temperature tube 2.1, so that the catalyst is convenient to fix, support and adjust the position and the filling height of the catalyst; the feed opening 2.4 is located between the first tube plate 2.21 and the second tube plate 2.22.

The thermostatic tube 2.1 is at least one or more of a light pipe (shown in fig. 1, 3, 4, 5 and 6), a finned tube (shown in fig. 2), a corrugated tube (shown in fig. 7), a wave coil (shown in fig. 8) and a trapezoidal tube (shown in fig. 9), a catalyst 2.11 is positioned in the thermostatic tube 2.1 (shown in fig. 1, 2, 3, 7, 8 and 9), the thermostatic tube of the present invention is not limited to the above types, and the purpose of the thermostatic tube is to effectively remove reaction heat and simultaneously assist other requirements; the selection of the type of the thermostatic tube depends on the raw materials and the proportion of methanol in the raw materials, the proportion of methanol is high, the heat generated in the reaction is high, a tube type with a large heat exchange area, such as a finned tube, and the generation temperature and pressure conditions of the required product (such as the trapezoidal tube has the change influence of volume and pressure) need to be selected, and meanwhile, whether the phenomena of expansion with heat and contraction with cold (such as the phenomena of expansion with heat and contraction with cold of a corrugated tube exist or not, the reaction pressure can be controlled, the activation temperature can be reduced, the adsorption performance of the catalyst can be improved, and the reaction effect can be enhanced) depends on the type.

Raw materials in the head tank 1 adopts the three-phase reaction for using methanol as basic raw materials, and the mixture of cooperation hydrocarbon and/or carbon monoxide and/or carbon dioxide and/or natural gas through controlling reactor bed temperature, and the raw materials that can convert simultaneously is diversified, and the product of conversion is diversified, the utility model discloses use methanol as basic raw materials, can cooperate hydrocarbon, carbon monoxide and carbon monoxide, carbon dioxide and natural gas etc. to mix the feeding wantonly.

One or more feed inlets are arranged between the first tube plate 2.21 and the second tube plate 2.22, when the number of the feed inlets is multiple, the feed inlets are arranged in a circumferential and/or vertical manner, the feed inlets distributed in the circumferential manner are used for uniformly heating the raw materials, and the feed inlets distributed in the vertical manner are used for effectively controlling the temperature gradient of the reaction; the constant temperature tube assembly 2.12 comprises a plurality of constant temperature tubes 2.1, a tube plate 2.2 and a catalyst fixer 2.3, wherein the number of the constant temperature tubes 2.1 is more than one; a large amount of heat released during the reaction in the tube is better transferred to the shell side, so that the reaction temperature is stable; the tube plate 2.2 is fixed on the side wall of the cylinder 2.6, and the constant temperature tube 2.1 is fixed on the tube plate 2.2; the constant temperature tube assemblies 2.12 in the tubular reactor 2 have one or more groups, and a fixed bed 2.10 is arranged in the tubular reactor 2 (as shown in fig. 1, 4, 5 and 6), so that devices and catalysts can be adjusted according to product requirements to meet the requirements of reaction conditions.

A circulation channel inlet 2.7 is arranged at the upper end of the cylinder body 2.6, a circulation channel outlet 2.8 is arranged on the side wall of the cylinder body 2.6, the circulation channel outlet 2.8 is arranged between the first tube plate 2.21 and the second tube plate 2.22 and is positioned at the upper part of the side wall of the cylinder body 2.6, the circulation channel outlet 2.8 is communicated with the circulation channel inlet 2.7 through a communicating pipeline (as shown in figures 1 and 2), and the discharged heat is removed by using raw materials and circulation materials, so that the circulation ratio is greatly reduced, and the temperature of a bed layer of the reactor is convenient to control; the light hydrocarbon produced by the reaction can be used as a power source for atomizing methanol and other raw materials, can consume part of reaction heat, can participate in the reaction, and improves the reaction conversion rate.

The gas lift pipes 2.9 are arranged in the cylinder body 2.6, the gas lift pipes are arranged in the cylinder body, heat loss is reduced, raw materials with lower original temperature can be heated to reach reaction temperature, the gas lift pipes 2.9 are positioned between two adjacent constant temperature pipes 2.1, the raw materials to be reacted are sufficiently heated through the flow guide of the gas lift pipes, and meanwhile, the effect of countercurrent temperature control on a catalyst in the constant temperature pipes is achieved, the gas lift pipes 2.9 are fixed on the first pipe plate 2.21, the upper ends of the gas lift pipes extend upwards out of the first pipe plate 2.21, the lower ends of the gas lift pipes 2.9 are positioned between the first pipe plate 2.21 and the second pipe plate 2.22, and the distance between the gas lift pipes and the second pipe plate 2.22 is adjustable;

The riser 2.9 is provided with a plurality of risers, the riser 2.9 is a light pipe or a finned pipe (shown in figures 3-9), the riser is arranged in the cylinder body, heat loss is reduced, the heating of raw materials with lower original temperature is facilitated to enable the raw materials to reach reaction temperature, the raw materials to be reacted are sufficiently heated by diversion of the riser, and meanwhile, the effect of countercurrent temperature control on a catalyst in the thermostatic tube is achieved; the raw material is positioned in the riser and needs to be heated, the thermostatic tube and the tube type of the riser are selected according to the needs, the thermostatic tube filled with the catalyst is a heat production center, and the heat needs to be removed through the riser.

catalyst 2.11 is a catalyst suitable for methanol reaction, and is at least one or more of ZSM-5, MTO-100, MAPSO molecular sieve and ELPSO molecular sieve.

the tubular reactor 2 is at least provided with a group of constant temperature tube assemblies, the tubular reactor 2 can be a combined reactor, and has various combination modes, at least one of a plurality of groups of constant temperature tube assemblies, a group of constant temperature tube assemblies and a group of fixed beds, a plurality of groups of constant temperature tube assemblies and a group of fixed beds, and a group of constant temperature tube assemblies 2.12 and a plurality of groups of fixed beds.

Other parts not described belong to the prior art.

Claims (10)

1. Hydrocarbon preparation equipment based on methanol normal temperature feeding reaction, which is characterized in that: adopting low-temperature direct feeding or atomized feeding below 100 ℃, and comprising a raw material tank (1), a tubular reactor (2), a condenser (3), a hydrocarbon product tank (4), a gas-liquid separator (5) and a communicating pipeline; the shell and tube reactor (2) comprises a cylinder (2.6), a constant temperature tube assembly (2.12) positioned in the cylinder (2.6), a feed inlet (2.4) arranged on the side wall of the cylinder (2.6) and a discharge outlet (2.5) arranged at the bottom of the cylinder (2.6); raw material tank (1) through the intercommunication pipeline with shell and tube reactor (2) intercommunication, condenser (3) are located shell and tube reactor (2) with between vapour and liquid separator (5), condenser (3) both ends respectively through the intercommunication pipeline with discharge gate (2.5) with vapour and liquid separator (5) intercommunication is located liquid discharge gate (5.1) of vapour and liquid separator (5) lower extreme lets in through the intercommunication pipeline hydrocarbon product jar (4), is located gaseous discharge gate (5.2) of vapour and liquid separator (5) upper end lets in through the intercommunication pipeline feed inlet (2.4).

2. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 1, characterized in that: the two transverse ends of the tube plate (2.2) are respectively fixed on the inner side wall of the cylinder (2.6); the number of the tube plates (2.2) is two, and the two tube plates are respectively a first tube plate (2.21) fixed at the upper part of the cylinder body (2.6) and a second tube plate (2.22) fixed at the lower part of the cylinder body (2.6); the upper end of the thermostatic tube (2.1) is fixed on the first tube plate (2.21) and extends upwards out of the first tube plate (2.21), and the lower end of the thermostatic tube is fixed on the second tube plate (2.22) and extends downwards out of the second tube plate (2.22); the catalyst fixer (2.3) is positioned at the end part of the constant temperature pipe (2.1); the feed opening (2.4) is located between the first tube plate (2.21) and the second tube plate (2.22).

3. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 2, characterized in that: the constant temperature pipe (2.1) is at least one of a light pipe, a finned pipe, a corrugated pipe and a trapezoid pipe, and a catalyst (2.11) is positioned in the constant temperature pipe (2.1).

4. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 3, characterized in that: the raw material in the raw material tank (1) is a mixture which takes methanol as a basic raw material and is matched with hydrocarbon and/or carbon oxide and/or carbon monoxide and/or carbon dioxide and/or natural gas.

5. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 4, characterized in that: one or more feed inlets are arranged between the first tube plate (2.21) and the second tube plate (2.22), and when the number of the feed inlets is multiple, the feed inlets are arranged in a circumferential and/or vertical manner; the constant temperature tube assembly (2.12) comprises a plurality of constant temperature tubes (2.1), tube plates (2.2) and catalyst holders (2.3), wherein the number of the constant temperature tubes (2.1) is more than one; the tube plate (2.2) is fixed on the side wall of the cylinder (2.6), and the constant temperature tube (2.1) is fixed on the tube plate (2.2); the thermostatic tube assembly (2.12) has one or more groups.

6. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 5, characterized in that: have circulation channel entry (2.7) to locate barrel (2.6) upper end, have circulation channel export (2.8) to locate on barrel (2.6) lateral wall, circulation channel export (2.8) are located between first tube sheet (2.21) and second tube sheet (2.22) and are located barrel (2.6) lateral wall upper portion, through the intercommunication pipeline intercommunication between circulation channel export (2.8) and the circulation channel entry (2.7).

7. the hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 6, characterized in that: the gas lift pipes (2.9) are arranged in the barrel body (2.6), the gas lift pipes (2.9) are positioned between two adjacent constant temperature pipes (2.1), the gas lift pipes (2.9) are fixed on the first pipe plate (2.21), the upper ends of the gas lift pipes extend upwards out of the first pipe plate (2.21), and the lower ends of the gas lift pipes (2.9) are positioned between the first pipe plate (2.21) and the second pipe plate (2.22) and the distance between the gas lift pipes and the second pipe plate (2.22) is adjustable.

8. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 7, characterized in that: the number of the gas lift pipes (2.9) is multiple, and the gas lift pipes (2.9) are light pipes or finned pipes.

9. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 8, characterized in that: the catalyst (2.11) is a catalyst suitable for methanol reaction, and is at least one or more of ZSM-5, MTO-100, MAPSO molecular sieve and ELPSO molecular sieve.

10. The hydrocarbon production equipment based on methanol normal-temperature feeding reaction as claimed in claim 9, characterized in that: the shell and tube reactor (2) is at least provided with a group of constant temperature tube assemblies (2.12), the shell and tube reactor (2) can be a combined reactor, and can be at least one of a plurality of groups of constant temperature tube assemblies (2.12), a group of constant temperature tube assemblies (2.12) and a group of fixed beds, a plurality of groups of constant temperature tube assemblies (2.12) and a group of fixed beds, a group of constant temperature tube assemblies (2.12) and a plurality of groups of fixed beds in various combination modes.