CN106929413B

CN106929413B - Brewing equipment and process for preparing alkane from chicken manure terpenized grass hydrocarbon

Info

Publication number: CN106929413B
Application number: CN201710115831.7A
Authority: CN
Inventors: 王丽华; 姜国文
Original assignee: Individual
Current assignee: Individual
Priority date: 2017-03-01
Filing date: 2017-03-01
Publication date: 2023-03-17
Anticipated expiration: 2037-03-01
Also published as: CN106929413A

Abstract

The invention belongs to the field of alkane brewing, and particularly relates to a brewing device and a process for preparing alkane by terpenizing grass hydrocarbon with chicken manure, which comprises a cross flow state reaction tube (1), a catalytic reaction tube (2), a distillation tube (3), a hydrocarbon gas flow state reforming generation unit (4), a double hydrogen conversion factor backflow seasoning column (5), a gas phase cavity (6), a liquid phase cavity (7), an encirclement thermal stress annular space tube (9), a difference frequency local oscillation column (11), a foam breaking net (12), a shell (13) and a difference frequency backflow unit (14); the upper ends of the hydrocarbon gas flow state reforming generation units (4) are respectively and fixedly communicated with the cross flow state reaction pipe (1), and the lower ends of the hydrocarbon gas flow state reforming generation units are respectively and fixedly communicated with the shell (13); the foam breaking net (12) comprises a first foam breaking net unit (1201) and a second foam breaking net unit (1202). The invention has the advantages of low energy consumption, low cost, low danger, high mass transfer efficiency and obvious environmental protection efficiency.

Description

Brewing equipment and process for preparing alkane from chicken manure terpenized grass hydrocarbon

Technical Field

The invention belongs to the field of alkane brewing, and particularly relates to a brewing device and a process for preparing alkane by terpenizing grass hydrocarbon with chicken manure.

Background

China faces multiple dilemmas in energy development. Firstly, china has abundant energy resources, but the number of people is small, and the per-person energy consumption and the per-person electric power are far lower than the average level in the world. Secondly, the energy distribution is very unbalanced. About 60.8 percent of coal exploration reserves in China are concentrated in North China, 70 percent of water energy resources are concentrated in the southwest and far away from consumption centers, and the enormous amount of petroleum and liquefied petroleum gas can cause railway transportation to be overwhelmed. Energy resources, energy production and economic layout are not coordinated, and north coal south transportation, west electricity east transportation and west gas east transportation are long-term patterns. Again, coal-based energy structures face significant challenges. China is a few countries which use coal as main energy in the world, compared with the world energy structure, china is seriously lack of petroleum and natural gas, the average value of the reserves of the petroleum and the natural gas is only 11 percent and 4 percent of the world average value respectively, the increase speed of the petroleum consumption in China is greatly higher than that of the petroleum production, and the petroleum supply prospect is severe.

The "congenital deficiency" of energy structure in our country is also the natural endowment we often say. Since this century, the total energy consumption of our country has risen rapidly, relying mainly on coal, petroleum and natural gas. At present, china becomes one of the largest energy consuming countries in the world, but the energy production capacity in China does not rise as fast as the consumption capacity in China, wherein the petroleum consumption growth speed is obviously higher than the domestic yield increase. Second only to the united states, china is the second largest petroleum consumer world country. The production of natural gas and non-fossil energy (hydroelectric, nuclear and aeolian) has increased rapidly in recent years, but the total amount is still limited. The investment of energy and related infrastructure is huge, the investment exceeds 2 trillion yuan RMB in 2010, the electric power construction accounts for more than half of the investment of all energy, and then the petroleum and natural gas exploitation and the petrochemical investment are performed again.

On the premise that the energy consumption of China is increased too fast, the resource environmental pressure of China is huge and hard to be sustained. On the premise that the demand continuously rises, the international energy price continuously rises, the problem of energy safety is continuously raised, and the domestic and foreign environmental constraints are met.

And the strength is continuously strengthened.

International petroleum resources are concentrated in a few countries, and the difficulty in mining is increasing. The increase of world petroleum yield is obviously restricted by international petroleum resources and geopolitical conditions, and can only be maintained to be increased by about 1 percent in average year.

At present, the oil refining process is a production process with high energy consumption, high cost and high danger. Part of oil field and industrial waste remains a considerable part of deposited heavy hydrocarbon resources. How to utilize the renewable materials is significant for solving the problems of energy shortage and environmental pollution.

Disclosure of Invention

The invention aims to overcome the defects of the prior art and provides the brewing equipment and the process for preparing the alkane from the chicken manure terpenic grass hydrocarbon, which have the advantages of low energy consumption, low cost, low risk, high mass transfer efficiency and remarkable environmental protection efficiency.

The present invention has been made to solve the above problems.

The brewing equipment for preparing alkane by chicken manure terpenized grass hydrocarbon comprises a cross flow state reaction pipe, a catalytic reaction pipe, a distillation pipe, a hydrocarbon gas flow state reforming generation unit, a double hydrogen conversion factor reflux seasoning column, a gas phase cavity, a liquid phase cavity, an encirclement thermal stress annular space pipe, a difference frequency local oscillation column, a foam breaking net, a shell and a difference frequency reflux unit; the hydrocarbon gas flow state reforming generation units are divided into two groups; each group comprises 4 columns, the upper ends of the 4 columns are respectively and fixedly communicated with the cross flow state reaction pipe, and the lower ends of the 4 columns are respectively and fixedly communicated with the shell; the foam breaking net is transversely and fixedly arranged in the shell, so that the inner cavity of the shell is divided into a gas phase cavity and a liquid phase cavity from top to bottom; the difference frequency local oscillation column is vertically connected with the lower part of the foam breaking net; the double hydrogen conversion factor backflow seasoning column is fixedly arranged on the shell and communicated with the inner cavity of the shell; two ends of the difference frequency backflow unit are respectively communicated with the top of the double hydrogen conversion factor backflow seasoning column and the inner cavity of the shell; two ends of the catalytic reaction tube are communicated with the cross flow state reaction tube; the distillation outlet pipe is communicated with the cross flow state reaction pipe; the heat stress filling annular space tube is fixedly arranged at the bottom of the shell; a temperature control sensing device is arranged at the upper part of the shell; the upper part of the shell is provided with an in-tank pressure regulator; the pressure regulator in the tank is provided with an electromagnetic valve; a pressure sensor is arranged at the upper part of the shell; the signal transmission port of the pressure sensor is communicated with the signal transmission port of the electromagnetic valve through the signal processing part; the foam breaking net comprises a first foam breaking net unit, a second foam breaking net unit and a third foam breaking net unit; the first foam breaking net unit, the second foam breaking net unit and the third foam breaking net unit are parallel to each other; and foam breaking columns are respectively and fixedly arranged between the first foam breaking net unit and the second foam breaking net unit as well as between the second foam breaking net unit and the third foam breaking net unit.

A brewing process for preparing alkane from chicken droppings terpene grass-grain hydrocarbon includes mixing (by weight percentage) biological peptide heavy hydrocarbon dissociating enzyme bihydrogen transfer factor modified cellulose (15%) which is prionized, modified and alkylated with 85% heavy hydrocarbon, brewing to obtain the product with lift force of 7 m, vaporizing at 288 deg.C, and thermal space not recombining according to the lift force ₈ -C ₂₄ Or greater than C ₈ -C ₂₄ One part of the hydrocarbon molecular groups is blocked by the gas flow state reforming generation unit and returns back through the foam breaking net, and the other part of the hydrocarbon molecular groups returns back through the dual hydrogen conversion factor reflux packing column and the foam breaking netFlowing, returning to liquid phase along the differential frequency local oscillation column, generating local oscillation of liquid phase fluid material in the tank due to temperature difference to promote enzymatic reaction, and recombining C in thermal space according to lifting force ₈ -C ₂₄ Hydrocarbon molecular groups are discharged through the gas flow state reforming generation unit, the cross flow state reaction pipe and the catalytic reaction pipe.

The invention has the advantages of low energy consumption, low cost, low danger, high mass transfer efficiency and obvious environmental protection efficiency. Through the optimal design of the foam breaking net, the mass transfer efficiency of the equipment is obviously improved. The production process which can be completed by a plurality of tall distillation towers and heating furnaces in the traditional oil refining process can be completed by one or a plurality of devices.

Drawings

The invention is further described with reference to the following figures and detailed description. The scope of the invention is not limited to the following expressions.

Fig. 1 is a schematic view of the internal structure of the present invention.

Fig. 2 is a side view of the present invention.

In the figure: 1. a cross-flow reaction tube; 2. a catalytic reaction tube; 3. a distillation pipe; 4. a hydrocarbon gas flow state reforming generation unit; 5. the double hydrogen conversion factor reflows to the seasoning column; 6. a gas phase chamber; 7. a liquid phase cavity; 8. a slag discharge port; 9. filling a thermal stress annular space tube; 10. a heat absorbing unit; 11. difference frequency local oscillation columns; 12. a foam breaking net; 13. a housing; 14. a difference frequency reflux unit; 15. a temperature control sensing device; 16. a tank internal pressure regulator; 17. a pressure sensor; 18. an electromagnetic valve; 19. a foam breaking column; 1201. a first foam breaking screen unit; 1202. a second foam breaking net unit; 1203. and the third foam breaking net unit.

Detailed Description

As shown in the figure, the tank for releasing internal energy of the organic medium fermented by the biological petroleum enzyme comprises a cross flow state reaction pipe 1, a catalytic reaction pipe 2, a distillation pipe 3, a hydrocarbon gas flow state reforming generation unit 4, a double hydrogen conversion factor reflux seasoning column 5, a gas phase cavity 6, a liquid phase cavity 7, an excess thermal stress annular space pipe 9, a difference frequency local oscillation column 11, a foam breaking net 12, a shell 13 and a difference frequency reflux unit 14; the hydrocarbon gas flow state reforming generation unit 4 is divided into two groups; each group comprises 4 columns, the upper ends of the 4 columns are respectively and fixedly communicated with the cross flow state reaction pipe 1, and the lower ends of the 4 columns are respectively and fixedly communicated with the shell 13; the foam breaking net 12 is transversely and fixedly arranged in the shell 13, so that the inner cavity of the shell 13 is divided into a gas phase cavity 6 and a liquid phase cavity 7 from top to bottom; the difference frequency local oscillation column 11 is vertically connected with the lower part of the foam breaking net 12; the double hydrogen conversion factor reflux seasoning column 5 is fixedly arranged on the shell 13 and is communicated with the inner cavity of the shell 13; two ends of the difference frequency backflow unit 14 are respectively communicated with the top of the double hydrogen conversion factor backflow seasoning column 5 and the inner cavity of the shell 13; the two ends of the catalytic reaction tube 2 are communicated with the cross flow state reaction tube 1; the distillation outlet pipe 3 is communicated with the cross flow state reaction pipe 1; the thermal stress interference annular space tube 9 is fixedly arranged at the bottom of the shell 13; a temperature control sensing device 15 is arranged at the upper part of the shell 13; a tank internal pressure regulator 16 is arranged at the upper part of the shell 13; an electromagnetic valve 18 is arranged on the tank internal pressure regulator 16; a pressure sensor 17 is arranged at the upper part of the shell 13; a signal transmission port of the pressure sensor 17 is communicated with a signal transmission port of the electromagnetic valve 18 through a signal processing part; the foam breaking net 12 comprises a first foam breaking net unit 1201, a second foam breaking net unit 1202 and a third foam breaking net unit 1203; the first foam breaking net unit 1201, the second foam breaking net unit 1202 and the third foam breaking net unit 1203 are parallel to each other; and foam breaking columns 19 are respectively and fixedly arranged between the first foam breaking net unit 1201 and the second foam breaking net unit 1202 as well as between the second foam breaking net unit 1202 and the third foam breaking net unit 1203.

According to the invention, the three-layer design is carried out on the foam breaking net, and the foam breaking column is adopted, so that the mass transfer efficiency of the equipment can be obviously improved, and the loss of valuable materials is reduced.

In the concrete operation, the hydrocarbon gas fluidized-state reforming generation unit 4 is filled with zirconia; alumina is filled in the catalytic reaction tube 2; niobium-molybdenum alloy is filled in the double hydrogen conversion factor reflux seasoning column 5. 30% of the grass hydrocarbon was mixed with 70% of the heavy oil and placed in the above-mentioned apparatus. Brewing C ₈ -C ₂₄ When the temperature reaches 84-284 ℃, the liquid is vaporized and fails to recombine C according to the lifting force in the hot space ₈ -C ₂₄ Or greater than C ₈ -C ₂₄ A part of the hydrocarbon molecular groups is fluidized by the gasThe whole generating unit 4 is blocked back and returns back through the foam breaking net 12, and the other part returns back through the hydrogen transfer factor returning seasoning column 5 and the foam breaking net 12. Most of the liquid phase returns to the liquid phase along the differential frequency local oscillation column 11, and the temperature difference between the fed back and returned hydrocarbon substances and the liquid phase is larger, so that the liquid phase fluid materials in the tank are subjected to local oscillation, the enzymatic reaction is accelerated, and the liquid phase fluid materials are recombined in a thermal space according to the lifting force C ₈ -C ₂₄ Hydrocarbon molecular group, through hydrocarbon gas fluid state reforming generation unit 4 filled with zirconia, cross fluid state reaction tube 1 and catalytic reaction tube 2 to produce refined C ₈ -C ₂₄ . The temperature control sensing device 16 of the invention can control the environmental temperature of the tank body; the pressure regulator in the tank can control the pressure parameter of the tank body.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. The brewing equipment for preparing alkane by utilizing chicken manure terpenized grass hydrocarbon is characterized by comprising a cross flow state reaction tube (1), a catalytic reaction tube (2), a distillation tube (3), a hydrocarbon gas flow state reforming generation unit (4), a double hydrogen conversion factor backflow seasoning column (5), a gas phase cavity (6), a liquid phase cavity (7), an excess thermal stress annular space tube (9), a differential frequency local oscillation column (11), a foam breaking net (12), a shell (13) and a differential frequency backflow unit (14); the hydrocarbon gas flow state reforming generation unit (4) is divided into two groups; each group comprises 4 columns, the upper ends of the 4 columns are respectively and fixedly communicated with the cross flow state reaction pipe (1), and the lower ends of the 4 columns are respectively and fixedly communicated with the shell (13); the foam breaking net (12) is transversely and fixedly arranged in the shell (13) to enable the inner cavity of the shell (13) to be divided into a gas phase cavity (6) and a liquid phase cavity (7) from top to bottom; the difference frequency local oscillation column (11) is vertically connected with the lower part of the foam breaking net (12); the double hydrogen conversion factor reflux seasoning column (5) is fixedly arranged on the shell (13) and is communicated with the inner cavity of the shell (13); two ends of the difference frequency backflow unit (14) are respectively communicated with the top of the double hydrogen conversion factor backflow seasoning column (5) and the inner cavity of the shell (13); the two ends of the catalytic reaction tube (2) are communicated with the cross flow state reaction tube (1); the distillation pipe (3) is communicated with the cross flow state reaction pipe (1); the filling thermal stress annular space tube (9) is fixedly arranged at the bottom of the shell (13); a temperature control sensing device (15) is arranged at the upper part of the shell (13); an in-tank pressure regulator (16) is arranged at the upper part of the shell (13); an electromagnetic valve (18) is arranged on the tank internal pressure regulator (16); a pressure sensor (17) is arranged at the upper part of the shell (13); a signal transmission port of the pressure sensor (17) is communicated with a signal transmission port of the electromagnetic valve (18) through a signal processing part; the foam breaking net (12) comprises a first foam breaking net unit (1201), a second foam breaking net unit (1202) and a third foam breaking net unit (1203); the first foam breaking net unit (1201), the second foam breaking net unit (1202) and the third foam breaking net unit (1203) are mutually parallel; and foam breaking columns (19) are respectively and fixedly arranged between the first foam breaking net unit (1201) and the second foam breaking net unit (1202) and between the second foam breaking net unit (1202) and the third foam breaking net unit (1203).

2. The process for preparing alkane brewing equipment from chicken manure terpenic grass-leaved hydrocarbon as claimed in claim 1, wherein the bio-peptide heavy hydrocarbon resolvase subjected to prionation and modified alkylation, 15% of double hydrogen transfer factor modified cellulose and 85% of heavy hydrocarbon are mixed and brewed, the lifting force is 7 m, the bio-peptide heavy hydrocarbon resolvase is vaporized when the temperature reaches 288 ℃, and C which cannot be recombined according to the lifting force in a hot space is obtained by vaporization ₈ -C ₂₄ Or greater than C ₈ -C ₂₄ One part of the hydrocarbon molecular group is blocked by the gas flow state reforming generation unit and flows back through the foam breaking net in a feedback way, the other part of the hydrocarbon molecular group flows back through the double hydrogen conversion factor backflow packing column through the foam breaking net in a feedback way, most of the hydrocarbon molecular group returns to the liquid phase along the difference frequency local oscillation column, and the liquid phase fluid material in the tank is subjected to local oscillation due to temperature difference, so that the enzymatic reaction is promoted, and the C is recombined in a thermal space according to the lifting force ₈ -C ₂₄ Hydrocarbon molecular group is passed through gas flow state reforming generation unit and cross flow state reaction tubeAnd the catalytic reaction tube is discharged.