CN2853768Y

CN2853768Y - Reaction furnace for preparing carbon disulfide by high pressure non-catalytic natural gas method

Info

Publication number: CN2853768Y
Application number: CN 200520144934
Authority: CN
Inventors: 李刚
Original assignee: LIAOYANG RUIXING CHEMICAL CO Ltd
Current assignee: LIAOYANG RUIXING CHEMICAL CO Ltd
Priority date: 2005-12-22
Filing date: 2005-12-22
Publication date: 2007-01-03
Anticipated expiration: 2015-12-22

Abstract

The utility model relates to a reacting furnace for carbon disulfide making in the way of high pressure and non-catalytic. The reacting furnace comprises a radiation section and a swashing section. The raw materials from the swashing section are transported to the furnace pipe to be preheated before getting heated in the radiation section. After that, raw materials lead out from the bottom of the radiation section. Refractory lining is installed in the radiation section. Several inflamers are set on the inside wall of the furnace body and the refractory lining. The furnace tube in the furnace chamber is heated mainly by the calorific radiation of the heated furnace lining, the fume advection and heat conduction. The fume generated by the burner is led into the swashing section by negative pressure and swashing heat exchange with the feeding furnace pipe is carried up. Behind the swashing section, a convective used to reclaim the used heat in the fume is optionally installed. After reclamation, the fume is ejected out from the chimney. The reacting furnace of the utility model with well-distributed heating has a high-usage of heat. The furnace tube has a long service life for two to ten years. And adjusting the production capacity is convenient.

Description

Reaction furnace for manufacturing carbon disulfide by high-pressure non-catalyticnatural gas method

Technical Field

The utility model relates to a carbon disulfide's apparatus for producing, in particular to adopt high pressure non-catalytic natural gas legal system to make carbon disulfide's reacting furnace, and utilize reacting furnace preparation carbon disulfide's production technology.

Background

Carbon disulfide is an important chemical raw material and is widely applied to production departments such as artificial fibers, pesticides, carbon tetrachloride, rubber, metallurgy and mineral separation, petroleum refining, military industry and the like. The current methods for preparing carbon disulfide can be roughly classified into the following methods according to raw material sources: firstly, the wood charcoal is prepared by reacting the wood charcoal with the sulfur, and the method can be simply divided into an external burning furnace method (such as an iron retort method) and an internal heating method (such as an electric furnace method) according to different heat sources, and because the method needs to consume a large amount of wood, the forest is protected along with the increase of the country, so that the method is greatly limited in the aspects of cost and raw material sources; secondly, charcoal substitutes such as coke or semicoke are used as raw materials to prepare the carbon disulfide, and the method is also limited by a plurality of adverse factors, such as higher ash content of the coke, dense carbon ring, lower yield and the like; thirdly, the natural gas is used as the raw material to prepare the carbon disulfide, compared with the former two, the raw material source is sufficient, and the technology is more advanced.

In the process of preparing carbon disulfide by using natural gas as a raw material, elemental sulfur is preheated and gasified under the condition of excessive sulfur, and S8 and S6 are decomposed into S2 to perform a carbon disulfide synthesis reaction with the natural gas. Liquid sulfur and natural gas generally flow from top to bottom in the reaction furnace, the liquid sulfur generally enters from the upper part of the furnace tube, and the natural gas generally enters from the upper part and the middle-lower part of the furnace tube; the sulfur vaporized in the furnace tubes reacts with the natural gas and is conducted out of the bottom of the furnace for further separation and collection of carbon disulfide. The carbon disulfide is prepared by a widely applied natural gas method at present, and whether the carbon disulfide is catalyzed or not and the high and low pressures are as follows: wherein the technology of catalytic synthesis is represented by PPG method; the technology of the low-pressure non-catalytic synthesis is represented by Stauffer technology of the American Stauffer company, and the technology of the high-pressure non-catalytic method is represented by an FMC method developed and improved by the American FMC company.

For the preparation of carbon disulfide by a natural gas method, whether high pressure and low pressure or catalysis exists or not, a reaction furnace is key equipment of the process and is also a part with the largest investment proportion, and how to prolong the service life of the furnace, prolong the production period, reduce the investment and improve the conversion rate of natural gas is a research hotspot in the field. The prior art reactors are typically designed in a circular or oval shape, the furnace tubes are typically designed in a coil arrangement, and the burners are typically located at the bottom of the reactor, so that the burners typically heat the upper and lower portions of the furnace unevenly. Because the burner needs to provide heat for the whole furnace, in order to provide a large amount of heat required by the sulfur vaporization at the upper part of the furnace tube, a strong hot-forcing zone is necessarily formed at the lower part of the furnace tube, and the carbon disulfide synthesis reaction occurs at the lower part of the furnace tube, and a large amount of heat is released in the synthesis reaction, so that the temperature of the furnace tube is overhigh, and the corrosivity of the sulfur to the furnace tube is remarkably increased when the temperature is overhigh, therefore, the service life of the furnace tube in the prior art is generally not more than 1 year, and the heat cannot be fully utilized. In view of the above disadvantages, chinese patent CN2568624Y discloses a reaction furnace with one or more burners located above the liquid sulfur inlet, which can heat from top to bottom, effectively provide heat in the sulfur vaporization process, and make use of the heat generated in the carbon disulfide synthesis process, thereby reducing the temperature difference between the upper and lower parts of the furnace tube and prolonging the service life of the furnace tube. The reaction furnace disclosed by the method is still in a traditional cylindrical shape, the furnace tube is still in a traditional coil tube type, the position of the burner is limited above the liquid sulfur inlet, the heat supply capacity is limited, the heat transfer of the reaction furnace is mainly realized by convection and conduction heat supply, although the temperature difference of the upper part and the lower part of the furnace tube is reduced to a certain extent, the horizontal temperature difference of the central temperature and the peripheral temperature of the furnace body still exists, the true uniform heat supply cannot be realized, and the furnace tube is still easy to coke and carbonize; meanwhile, the scale enlargement of the reaction furnace is not easy to realize due to the limited heat supply capacity of the reaction furnace. Meanwhile, because the flue gas discharge port of the reaction furnace is positioned at the bottom of the reaction furnace, additional equipment cost such as a fan is needed, and the waste heat cannot be fully utilized.

SUMMERY OF THE UTILITY MODEL

Based on the defects existing in the prior art, the utility model aims to provide a high-pressure non-catalytic reaction furnace which has more reasonable structure, more uniform heat supply, longer service life and higher natural gas conversion rate.

The utility model relates to a reaction furnace, have the radiation section and swash the section, the raw materials gets into the boiler tube by swashing the section and preheats, and then be heated in the radiation section, derive the stove by radiation section bottom, the radiation section sets up the refractory furnace wall, set up a plurality of combustors in the lateral wall of radiation section furnace body and furnace wall, boiler tube in the furnace mainly heats through the convection current and the heat-conduction of the thermal radiation and the flue gas that are heated the furnace wall, the flue gas that the combustor produced leans on the leading-in swashing section of pressure, swash the heat transfer with the feeding boiler tube that swashs in the section, can select after swashing the section to set up the waste heat in the convection section in order to retrieve the flue gas, the waste heat can be used for producing steam for example, flue gas after retrieving the waste heat is discharged through the chimney, swashing section and the selectable of reaction furnace wall set up.

The utility model is right the reacting furnace, purify natural gas and liquid sulphur and can get into the reacting furnace in the different positions of swashing the section, the preferred natural gas that purifies is higher than the liquid sulphur entry in the entry position of swashing the section, and the natural gas after preheating is direct to converge with the liquid sulphur that gets into, has prolonged the contact time of natural gas and liquid sulphur in the boiler tube, has reduced the production of natural gas carbon deposit in the boiler tube, has improved the conversion of reaction.

The furnace tube of the reaction furnace adopts a heat-resistant alloy casting tube, such as a chromium-nickel alloy series, preferably HK40 or HP 40; the lining is made of a refractory material, preferably refractory brick or refractory felt.

Adopt the process of square reacting furnace carbon disulfide production as follows: the purified natural gas enters an impulse section of the reaction furnace, is preheated to 300-500 ℃ and then is mixed with liquid sulfur entering the impulse section, sulfur is rapidly heated, pyrolyzed and vaporized in the impulse section, the mixed reactant is conveyed to a radiation section through a furnace tube, a side wall burner burns a furnace lining in the radiation section, the furnace tube is heated through convection and heat conduction of furnace lining radiation and flue gas, the reactant in the furnace tube is heated to 550-700 ℃ in the section, a non-catalytic synthesis reaction occurs, and carbon disulfide and hydrogen sulfide are generated, and the reaction equation is as follows:

the reaction product is withdrawn from the bottom of the furnace to further separate the carbon disulfide and hydrogen sulfide byproduct. The flue gas in the side wall burner is guided into the impulse section by pressure to generate impulse heat transfer with the natural gas and liquid sulfur feeding pipe,and then the flue gas can enter a convection section, and the flue gas is cooled by recovering waste heat through a heat exchange medium in the convection section and then discharged through a chimney.

As the utility model discloses preferred technical scheme, the lateral wall combustor layering sets up, the combustor quantity of each layer can be the same also can be different, the heat that preferred each layer combustor provided suits with the heat load that the relevant position needs, the quantity of each layer combustor is decided by the heat load of each layer position department promptly, because need consider at radiation section upper portion heat load and swap required sensible heat of section natural gas preheating, the required sensible heat of liquid sulfur gasification pyrolysis, latent heat, reaction heat etc. consequently, its heat load is the biggest, and from radiation section upper portion to radiation section lower part, because the synthesis reaction has taken place, the synthesis reaction heat is constantly released, consequently required heat load can correspondingly reduce. Therefore, the burners are arranged in layers and are adapted to the heat load at the positions, so that the heating uniformity and the heat utilization rate of the furnace can be obviously improved, the service life of the furnace tube is prolonged, and the yield is improved.

The furnace body of the existing reaction furnace adopts a circular or oval shape, and the side wall has radian, so that the combustor can not effectively and uniformly burn the furnace lining. Therefore as the utility model discloses further preferred technical scheme, the furnace body adopts the ladder type structure or for box structure, adopts the structure, the setting and the adjustment of the combustor of being convenient for very much on the stove lateral wall are convenient for adjust the productivity ofreacting furnace as required.

As the utility model discloses in the more preferred technical scheme of step further, the boiler tube adopts the calandria to arrange at the radiation section, arranges the tubulation for the coil pipe type and arranges that the distance that makes the boiler tube apart from the furnace both sides furnace lining equals, is heated more evenly, and life is longer.

The quantity of the lateral wall combustor of reacting furnace is decided by required heat load, can adjust according to the productivity, and evenly distributed is at the furnace lateral wall, and it is more reasonable to burning thermal utilization, and make full use of multiple heat transfer modes such as radiation, conduction, convection current on heat transfer mode, and the heating capacity is strong, and being heated of boiler tube is more even, and difficult coking carbon deposit, boiler tube life-span reaches 2 ~ 10 years. Adopt the reaction furnace carries out synthetic reaction yield of carbon disulfide height, and the scale enlargement of reaction furnace easily realizes moreover.

Drawings

FIG. 1A is a side view of the furnace body of the box-type carbon disulfide reaction furnace of the present invention

FIG. 1B is a front view of the furnace body of the box-type carbon disulfide reactor of the present invention

FIG. 2A is a side view of the trapezoidal carbon disulfide reaction furnace body of the present invention

FIG. 2B is a front view of the trapezoidal carbon disulfide reactor body of the present invention

In the figure, 1-radiation section, 2-impulse section, 3-convection section, 4-furnace lining, 5-burner, 6-furnace tube,7-natural gas inlet, 8-liquid sulfur inlet, 9-product outlet, 10-chimney and 11-furnace body support.

Detailed Description

The present invention will be further described with reference to the following detailed description.

Example 1: fig. 1A and 1B show a schematic structural view of a box-type carbon disulfide reactor according to the present invention, wherein the production capacity of the reactor is 1.5 ten thousand tons/year, fig. 1A is a side view of the box-type reactor, and fig. 1B is a front view of the box-type reactor. As can be seen from the figure, the reaction furnace is provided with a radiation section 1, an impulse section 2 and a convection section 3, the radiation section 1 is box-shaped, furnace linings 4 are arranged in the furnace bodies of the radiation section 1 and the impulse section 2, the furnace linings are built by refractory bricks or refractory felts, 14 combustors 5 are arranged on the side wall of the radiation section in three layers according to the heat load required by capacity, furnace tubes 6 in the reactor are arranged in a calandria manner, the furnace tubes are made of HK40 heat-resistant alloy cast tubes, the inlet 7 of natural gas at the impulse section is slightly higher than the liquid sulfur inlet 8, and the furnace tubes 6 are provided with an outlet 9 at the bottom of the radiation section. When the reactor works, firstly, natural gas enters the impulse section for preheating through the inlet 7, sulfur enters the impulse section for preheating, pyrolysis and gasification through the inlet 8, the natural gas and the sulfur are converged in the impulse section and enter the radiation section 1, the burner 5 on the side wall of the furnace body of the radiation section 1 heats the furnace tube 6 through furnace lining radiation and flue gas convection conduction, high-pressurenon-catalytic synthesis reaction occurs in the furnace tube 6, and a reaction product is led out of the reactor from the bottom product outlet 9 for further separation; high-temperature flue gas is introduced into the impulse section 2 through pressure, and collides with a feeding pipeline in the impulse section 2 to carry out impulse heat exchange, then rises to enter the convection section 3 to recover waste heat, and the flue gas is discharged through a chimney 10.

Example 2: the attached figures 2A and 2B show the structure schematic diagram of the trapezoidal carbon disulfide reaction furnace of the invention. The reaction furnace had a production capacity of 3.5 ten thousand tons/year, wherein fig. 2A is a side view of the ladder type reaction furnace and fig. 2B is a front view of the ladder type reaction furnace. With reference to its side view, it is known that the radiant section 1 of the reactor has a trapezoidal section, more specifically in the present example it has a three-layer trapezoidal superimposed section. The reaction furnace also comprises a furnace body consisting of a radiation section 1, an impact section 2 and a convection section 3, and the furnace body is supported by a furnace body support 11. Furnace linings 4 are arranged in the furnace bodies of the radiation section 1 and the impulse section 2, the furnace linings are built by refractory bricks or refractory felts, 40 burners 5 are arranged on the side wall of the radiation section in three layers according to the heat load required by capacity, furnace tubes 6 in the reactors are arranged in a calandria manner, the furnace tubes are made of HP40 heat-resistant alloy casting tubes, the inlets 7 of the natural devices in the impulse section are slightly higher than liquid sulfur inlets 8, and the bottom of the radiation section of the furnace tubes 6 is provided with product outlets 9. When the reactor works, firstly, natural gas enters the impulse section throughthe inlet 7 for preheating, sulfur enters the impulse section through the inlet 8 for preheating, pyrolysis and gasification, the sulfur and the natural gas are converged in the impulse section and enter the radiation section 1, the burner 5 on the side wall of the furnace body of the radiation section 1 heats the furnace tube 6 through furnace lining radiation and flue gas convection conduction, a high-pressure non-catalytic synthesis reaction occurs in the furnace tube 6, and a reaction product is led out of the reactor from the bottom outlet 9 to further separate the product; the high-temperature flue gas is introduced into the impulse section by pressure, collides with a feeding pipeline in the impulse section, carries out impulse heat exchange, then rises to enter the convection section to recover waste heat so as to generate steam, and the flue gas is discharged from a chimney 10.

Although the present invention has been described with reference to the preferred embodiments, it is not intended to be limited thereto, and those skilled in the art can make equivalent changes and modifications without departing from the spirit and scope of the present invention.

Claims

1. The utility model provides a high-pressure non-catalytic carbon disulfide reacting furnace, has radiation section and swashs the section, swashs the section and is located radiation section upper portion, and the raw materials gets into the boiler tube by swashs the section, and then is heated at the radiation section, derives the stove by radiation section bottom, its characterized in that: the radiant section is provided with a refractory furnace lining, a plurality of burners are arranged in the side wall between the furnace body of the radiant section and the furnace lining, the furnace tubes are heated in the modes of radiation, conduction and convection, and the flue gas generated by the burners is led into the impulse section by pressure and led out after impulse heat exchange with the feeding furnace tubes in the impulse section.

2. The reactor according to claim 1, characterized in that a convection section is arranged after the sloshing section for recovering the residual heat in the flue gas, and a refractory lining is arranged in the sloshing section and/or the convection section.

3. The reactor according to claim 1 or 2, wherein the side wall burners are arranged in layers in the radiant section, and the number of burners in each layer is the same or different.

4. The reactor according to claim 3, wherein the heat supplied by each burner is adapted to the heat load required at the corresponding location.

5. The reactor according to claim 1 or 2, characterized in that natural gas and liquid sulfur enter at different positions of the impulse section, and the natural gas is preheated and then joined with the entering liquid sulfur.

6. The reactor furnace of claim 5, wherein the natural gas inlet is higher than the liquid sulfur inlet.

7. The reactor of claim 1 or 2, wherein the furnace tubes are arranged in a calandria configuration in the radiant section.

8. The reaction furnace according to claim 1 or 2, wherein the furnace tube is a heat-resistant alloy cast tube.

9. The reactor of claim 8, wherein said heat-resistant alloy cast tube is HK40 or HP 40.

10. The reaction furnace of claim 1 or 2, wherein the reaction furnace is a ladder or a box.

11. A reactor furnace as claimed in claim 1 or claim 2 in which the refractory lining is made of a refractory material.

12. The reactor of claim 11, wherein the refractory material is a refractory brick or a refractory felt.