Fluidized bed synthesis production circulating energy-saving method

Abstract

The present application relates to a kind of circulating energy-saving methods of fluidized bed synthesis production, step 1: the raw material in liquid raw material tank is input into vaporizer, raw material is first gasified after passing through vaporizer and then input into superheater, form superheated gas;Step 2: solid particles are sent into fluidized bed reactor, while superheated gas enters from the bottom of fluidized bed reactor, and reaction occurs with solid particles;Step 3: the gas that is not completely reacted carries synthesis crude product, fine solid particles powder into dry dedusting system together;Step 4: after wet dedusting, excess gas and crude product are separated by cooler, and the raw material gas evaporated in product refining equipment rectification process is transported back to the pipeline between vaporizer and superheater;Step 5: gas rectification recovery system returns the raw material gas after rectification to the pipeline between vaporizer and superheater.The present application can reduce gasification and liquefaction process, reduce the amount of heat and refrigerant, without inert gas intervention during vaporizer failure switching, and the system has strong risk resistance.

Description

TECHNICAL FIELD

[0001] The present application relates to a kind of fluidized bed synthesis production cycle energy-saving method. BACKGROUND

[0002] The existing fluidized bed synthesis is using excess raw material circulation scheme, after refining by rectifying column, condense into liquid state and re-enter the system, because synthesis raw material is greatly excessive, the number of raw material to be recovered is huge, after cooling, raw material returns to production system and needs to be gasified again to enter the synthesis system, condensation of refining system will bring pressure to cooling system, and gasification will increase the consumption of heat energy. Abnormal conditions such as vaporizer failure and inert gas stop may occur during production, which brings risks to stable production of the production system. SUMMARY

[0003] The purpose of the present application is to provide a kind of fluidized bed synthesis production cycle energy-saving method, which can realize the recycling of synthesis gas and achieve the purpose of energy saving and consumption reduction.

[0004] The purpose of the present application is achieved by the following technical scheme: a kind of fluidized bed synthesis production cycle energy-saving method, comprising the following steps:

[0005] Step 1: input the raw material in the liquid raw material tank into the vaporizer, the raw material is first gasified by the vaporizer and then overheated by the superheater to form superheated gas;

[0006] Step 2: send the solid particles into the fluidized bed reactor, at the same time, the superheated gas enters from the bottom of the fluidized bed reactor and reacts with the solid particles;

[0007] Step 3: the unreacted gas carries the crude product and fine solid particle powder into the dry dedusting system, and then through the wet dedusting system, wherein the fine solid particle powder separated by the dry dedusting system returns to the fluidized bed reactor to continue to participate in the synthesis reaction;

[0008] Step 4: separate the excess gas and the crude product by the cooler after wet dedusting, the crude product enters the product refining equipment, and the evaporated raw material gas in the rectification process of the product refining equipment is transported back to the pipeline between the vaporizer and the superheater, and then reenters the fluidized bed reactor for reaction after overheating; and the excess gas enters the gas rectification recovery system, and the gas rectification recovery system transports the concentrated crude product liquid in the rectifying column back to the product refining equipment;

[0009] Step 5: the raw material gas after rectification is returned to the pipeline between the vaporizer and the superheater by the gas rectification recovery system, and then reenters the fluidized bed reactor for reaction after overheating, and the remaining raw material gas enters the recovery material condenser and returns to the liquid raw material tank after condensation.

[0010] Further, the vaporizer comprises a vaporizer A and a vaporizer B, which are connected in parallel with each other; the superheater comprises a superheater A and a superheater B, which are connected in parallel with each other.

[0011] Further, the raw material gas in the product refining equipment distillation process is returned to the fluidized bed reactor after the gas distillation recovery system distillation, and the vaporization amount of the vaporizer is reduced synchronously to meet the consumption.

[0012] Further, the fine solid particle powder not removed in the dry dust removal system enters the liquid in the wet dust removal system and is discharged at the bottom of the washing tower.

[0013] Further, the non-condensable tail gas in the gas distillation recovery system is discharged at a high altitude or water washed.

[0014] Compared with the prior art, the present application has the following advantages:

[0015] The liquid needs to absorb a large amount of heat in the gasification process, and needs a heat source to supply heat; the gas needs to release a large amount of heat when condensing, and needs a coolant to lead out the heat. The raw material gas in the product refining equipment distillation process and the raw material gas after the gas distillation recovery system distillation are returned to the fluidized bed reactor for cyclic reaction, which can reduce the gasification and liquefaction process and reduce the use amount of heat and coolant.

[0016] At the same time, various emergency situations will occur in production, affecting the smooth progress of production, especially the risk of material interruption. In the present application, the raw material can be directly returned to the system, although the amount is not enough for normal conditions, but it is enough for the use amount required for low-load production, so as to ensure normal production when the vaporizer fails.

[0017] The present application effectively reduces the steam consumption, which is originally about 5 tons per hour, to about 2 tons per hour. At the same time, no inert gas is needed during the switching period of the vaporizer failure, and the risk resistance of the system is significantly enhanced. BRIEF DESCRIPTION OF DRAWINGS

[0018] Figure 1 is a flowchart of a fluidized bed synthesis production circulating energy-saving method of the present application. DETAILED DESCRIPTION

[0019] The content of the present application will be described in detail below in combination with the drawings and examples in the specification:

[0020] As Figure 1 shown is an embodiment schematic diagram of a fluidized bed synthesis production circulating energy-saving method provided by the present application.

[0021] A fluidized bed synthesis production circulating energy-saving method, comprising the following steps:

[0022] Step 1: The raw materials in the liquid raw material tank are input into the vaporizer, and the raw materials are first vaporized in the vaporizer and then overheated in the superheater to form superheated gas, which enters the fluidized bed to participate in the synthesis reaction and forms a fluidized bed effect;

[0023] The type of recycled raw material in the synthesis reaction is liquid under normal storage, and the raw material that needs to be vaporized during production.

[0024] The raw materials include chloromethane, dichloromethane, methanol, ethanol and other low-boiling-point synthesis raw materials.

[0025] The vaporizer includes vaporizer A and vaporizer B, which are connected in parallel with each other; the superheater includes superheater A and superheater B, which are connected in parallel with each other.

[0026] Step 2: The solid particles are sent into the fluidized bed reactor, while the superheated gas enters from the bottom of the fluidized bed reactor and reacts with the solid particles;

[0027] Step 3: The unreacted gas carries the crude synthesis product and fine solid particle powder into the dry dust removal system, and then passes through the wet dust removal system, wherein the fine solid particle powder separated by the dry dust removal system returns to the fluidized bed reactor to continue participating in the synthesis reaction;

[0028] The fine solid particle powder that is not completely removed in the dry dust removal system enters the liquid in the wet dust removal system and is discharged at the bottom of the washing tower.

[0029] Step 4: After wet dust removal, the excess gas and the crude product are separated by the cooler, the crude product enters the product refining equipment, and the evaporated raw material gas is transported back to the pipeline between the vaporizer and the superheater during the rectification process of the product refining equipment. After being overheated, it reenters the fluidized bed reactor for reaction; and the excess gas enters the gas rectification recovery system, which transports the concentrated crude product liquid in the rectification tower back to the product refining equipment;

[0030] Step 5: The raw material gas after rectification is returned to the pipeline between the vaporizer and the superheater, and after being overheated, it reenters the fluidized bed reactor for reaction, and the remaining raw material gas enters the recovery material condenser and is returned to the liquid raw material tank after condensation.

[0031] The excess raw material gas after synthesis is recovered and refined without condensation and directly returned to the rectification system. According to the working condition, it can be returned to one recovery refining tower, or it can be returned together with the raw material gas collected from the top of the product refining tower. Due to the difference in tower pressure operation, when returned simultaneously, the pressure operation needs to be lower than the outlet pressure of the vaporizer, but slightly higher.

[0032] The non-condensable tail gas in the gas rectification recovery system is discharged at high altitude or treated by water washing.

[0033] After the raw gas in the product refining equipment rectification process returns to the fluidized bed reactor or the raw gas after the gas rectification recovery system rectification returns to the fluidized bed reactor, the vaporization amount of the vaporizer is simultaneously reduced to meet the consumption.

[0034] The embodiment can be applied to the synthesis of monomers from silicon powder and chloromethane in organosilicon, and the method is practically verified to be feasible.

[0035] The application includes but is not limited to a gas-solid phase reactor, and a gas-liquid phase reactor can also be used after fine adjustment.

Claims

1. A fluidized bed synthesis production cycle energy saving method, characterized in that, It comprises the following steps: Step 1: input the raw material in the liquid raw material tank into the vaporizer, and then input the raw material into the superheater after being vaporized in the vaporizer to form superheated gas; Step 2: send the solid particles into the fluidized bed reactor, and at the same time, the superheated gas enters from the bottom of the fluidized bed reactor and reacts with the solid particles; Step 3: the unreacted gas carries the synthesized crude product and fine solid particle powder into the dry dust removal system, and then passes through the wet dust removal system, wherein the fine solid particle powder separated by the dry dust removal system returns to the fluidized bed reactor to continue to participate in the synthesis reaction; Step 4: after wet dust removal, the excess gas and the crude product are separated by the cooler, the crude product enters the product refining equipment, and the evaporated raw material gas is transported back to the pipeline between the vaporizer and the superheater during the rectification process of the product refining equipment, and then reenters the fluidized bed reactor after being superheated; and the excess gas enters the gas rectification recovery system, and the gas rectification recovery system transports the concentrated crude product liquid in the rectification tower back to the product refining equipment; Step 5: the raw material gas after rectification by the gas rectification recovery system returns to the pipeline between the vaporizer and the superheater, and then reenters the fluidized bed reactor after being superheated, and the remaining raw material gas enters the recovery material condenser and returns to the liquid raw material tank after being condensed.

2. The fluidized bed synthesis production cycle energy saving method according to claim 1, characterized in that: The vaporizer comprises a vaporizer A and a vaporizer B, and the vaporizer A and the vaporizer B are connected in parallel with each other; the superheater comprises a superheater A and a superheater B, and the superheater A and the superheater B are connected in parallel with each other.

3. The fluidized bed synthesis production cycle energy saving method according to claim 1, characterized in that: The raw material gas returned to the fluidized bed reactor during the rectification process of the product refining equipment or the raw material gas returned to the fluidized bed reactor after being rectified by the gas rectification recovery system is simultaneously adjusted to a smaller vaporization amount, so that it can meet the consumption.

4. The fluidized bed synthesis production cycle energy saving method according to claim 1, characterized in that: The fine solid particle powder not completely removed in the dry dust removal system enters the liquid in the wet dust removal system and is discharged at the bottom of the washing tower.

5. The fluidized bed synthesis production cycle energy saving method according to claim 1, characterized in that: The incondensable tail gas in the gas rectification recovery system is discharged at a high altitude or treated by water washing.

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